Helium Recovery From Streams Containing Helium, Carbon Dioxide, and at least one of Nitrogen and Methane

ABSTRACT

Systems and methods are provided for recovering helium from a feed comprising helium, carbon dioxide, and at least one of nitrogen and methane. The feed is separated in a first separator to form helium-enriched stream and a CO 2 -enriched stream. The helium-enriched stream is separated in a pressure swing adsorption unit to form a helium-rich product stream and a helium-lean stream. At least a portion of the helium-lean stream is recycled to the first separator with the feed. In some embodiments, a membrane separation unit is used to enhance helium recovery.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation-in-part of U.S. patent applicationSer. No. 13/564,871, filed Aug. 2, 2012, incorporated herein byreference.

BACKGROUND OF THE INVENTION

The present invention provides systems and methods for obtaininghelium-rich product fractions from feed streams containing carbondioxide and at least one of nitrogen and methane.

There are many high-pressure gas fields that supply carbon dioxide-richgas streams for the oil and gas industry. In general, the carbon dioxide(CO₂) content of these streams is greater than 50% by volume, andusually from about 60 to about 98 vol %. In addition, the gas mixturetypically contains methane (for example from about 0.1 to about 20 vol%), nitrogen (up to about 30 vol %), small amounts of argon, hydrogen,and heavier hydrocarbons, and helium fractions up to about 1% by volume.These CO₂-rich gas streams have been used in the industry for enhancedoil recovery (EOR), and the associated hydrocarbons are optionallyrecovered when economically justified.

Helium is used in a variety of applications, including for examplecryogenic processes, pressurizing and purging systems, maintainingcontrolled atmospheres, and welding. Since helium is becomingincreasingly scarce, however, new ways to recover helium are beingconsidered, including recovering the small amounts of helium containedin such CO₂-rich streams. In order to do so, a product stream must berecovered that has a sufficient composition and pressure for furthertreatment in a helium purification and liquefaction process. Therecovered helium-rich product fraction, then, should have a heliumcontent of at least about 35 vol % in nitrogen, preferably greater than50 vol %, with only trace amounts of CO₂.

Because the triple point of CO₂ is −56.6° C., purification processesthat rely on phase separation carried out by means of a low temperaturedistillation process can perform only a coarse separation of the CO₂from a feed gas mixture. CO₂ separation can also be carried out by othermethods, such as amine scrubbing, methanol scrubbing, or adsorptionprocesses such as pressure swing adsorption (PSA), but an improvedprocess that maximizes recovery of helium and CO₂ and minimizes powerrequirements is commercially and economically desirable.

U.S. Pat. No. 3,653,220 describes recovery of helium from a naturalgas-containing feed in which CO₂ in the feed (approximately 22 vol %) isremoved using a CO₂ PSA upstream of a low temperature separation unit.Recovering helium from a natural gas feed, however, is simpler thanrecovering helium from a feed having greater than 50 vol % CO₂, becausecryogenic separation may be employed earlier in the recovery process toproduce pure helium.

U.S. Pat. No. 3,740,962 is similar to the previous process, except thatCO₂ is removed from a natural gas feed using an amine scrubbing unit,and crude helium is then separated from a predominantly methane streamvia a cryogenic separation process using external refrigerants tocondense the feed gas.

WO 2010/060533 describes bulk separation of CO₂ from a helium-containingnatural CO₂ source using a low temperature separation process, withfurther downstream helium purification. DE 102008007925 describesrecovery of helium from a feed containing helium, nitrogen, and methaneby partial condensation of the feed and subsequent separation intohelium-rich and helium-lean fractions.

The present invention provides an improved process for recovering heliumfrom a CO₂ feed while preferably recovering at least 98% of the heliumin the feed to the helium product, preferably recovering at least 99% ofthe CO₂ in the feed back to the pipeline, minimizing power requirements,and meeting the CO₂ composition requirements of a downstream pipeline byoptionally rejecting nitrogen within the helium recovery process.

BRIEF SUMMARY OF THE INVENTION

The present invention provides systems and methods for recovering heliumfrom a feed comprising helium, carbon dioxide, and at least oneintermediate component having a volatility between those of helium andcarbon dioxide, for example, nitrogen and methane.

Some embodiments of the present invention comprise separating the carbondioxide and the components of intermediate volatility from the helium ata temperature greater than −82.7° C. to form a helium-rich productstream, wherein the concentration of at least one of the intermediatecomponents in the helium-rich product stream is lower than itsconcentration in the feed stream, and wherein at least part of theseparation is effected by contacting a vapor with a liquid.

Embodiments of the present invention for recovering helium from a feedstream comprising helium and at least 50 mol % CO₂ comprise: (i) a firstseparator comprising a distillation column, configured to separate thefeed stream into a first helium-enriched stream and a first CO₂-enrichedstream, wherein at least part of the feed stream enters the distillationcolumn at an intermediate location; (ii) one or more heat exchangersconfigured to cool the feed stream and heat the first helium-enrichedand first CO₂-enriched streams; (iii) a second separator configured toseparate a portion of the first CO₂-enriched stream into a liquidfraction and a vapor fraction and recycle the liquid fraction to the topof the distillation column; (iv) a compressor configured to compress thenon-separated portion of the first CO₂-enriched stream and the vaporfraction of the separated portion of the first CO₂-enriched stream toform a CO₂-rich product stream; and optionally (v) a third separatorconfigured to separate the first helium-enriched stream to form ahelium-rich product stream and a helium-lean stream.

Embodiments of the present invention for recovering helium from a feedstream comprising helium, carbon dioxide, and at least one of methaneand nitrogen comprise: (i) a separator (a fractionator or pressure swingadsorption unit) operatively configured to separate a separator feedstream comprising at least a portion of the feed stream into a firsthelium-enriched stream and a first CO₂-enriched stream; (ii) a pressureswing adsorption unit operatively configured to separate a pressureswing adsorption unit feed stream into a helium-rich product stream anda helium-lean stream where the pressure swing adsorption unit feedstream comprises at least a portion of the first helium-enriched stream;(iii) a compressor operatively disposed to receive a compressor feedstream and operatively configured to compress the compressor feed streamto form a compressor effluent stream, where the compressor feed streamcomprises the helium-lean stream and a helium-enriched permeate stream;and (iv) a membrane separation unit operatively disposed to receive afirst portion of the compressor effluent stream and operativelyconfigured to separate the first portion of the compressor effluentstream into the helium-enriched permeate stream and a helium-depletednon-permeate stream, where (v) the separator is also operativelydisposed to receive a second portion of the compressor effluent stream.

The systems and methods of the present invention can provide greaterthan 98% recovery of the helium in the feed stream to a helium productstream and preferably greater than 99% recovery of the CO₂ in the feedstream to a CO₂ product stream. Further, systems and methods of thepresent invention may be configured to minimize power requirements,minimize equipment size, and meet downstream CO₂ pipeline compositionrequirements through the use of an intermediate column reboiler, a CO₂wash stream fed to the top of the distillation column, and/or rejectionof nitrogen from the process. Some embodiments of the present inventionare particularly well-suited for retrofit applications.

BRIEF DESCRIPTION OF SEVERAL VIEWS OF THE DRAWINGS

FIG. 1 is a schematic diagram of a helium recovery system incorporatingmultiple flash separators.

FIG. 2 is a schematic diagram of a helium recovery system incorporatinga stripping column.

FIG. 3 is a schematic diagram of an embodiment of the inventionincorporating a distillation column with a CO₂ wash stream.

FIG. 4 is a schematic diagram of an embodiment of the inventionincorporating a distillation column with a CO₂ wash stream and nitrogenrejection.

FIG. 5 is a schematic diagram of an embodiment of the inventionincorporating catalytic combustion to increase helium purity in thehelium product stream.

FIG. 6 is a schematic diagram of an embodiment of the inventionincorporating a distillation column with a recycle CO₂ wash streamwithout additional helium purification downstream of the distillationcolumn.

FIG. 7 is a schematic diagram of an embodiment of the inventionincorporating a distillation column with a CO₂ wash stream derived fromthe feed stream without additional helium purification downstream of thedistillation column.

FIG. 8 is a schematic diagram of a helium recovery system incorporatinga membrane separation unit.

FIG. 9 is a schematic diagram of a helium recovery system for comparingwith the helium recovery system of FIG. 8.

DETAILED DESCRIPTION OF THE INVENTION

The ensuing detailed description provides exemplary embodiments only,and is not intended to limit the scope, applicability, or configurationof the invention. Rather, the ensuing detailed description of theexemplary embodiments will provide those skilled in the art with anenabling description for implementing the embodiments, it beingunderstood that various changes may be made in the function andarrangement of elements without departing from scope of the invention asdefined by the claims.

The articles “a” and “an” as used herein mean one or more when appliedto any feature described in the specification and claims. The use of “a”and “an” does not limit the meaning to a single feature unless such alimit is specifically stated. The article “the” preceding singular orplural nouns or noun phrases denotes a particular specified feature orparticular specified features and may have a singular or pluralconnotation depending upon the context in which it is used.

The adjective “any” means one, some, or all, indiscriminately ofwhatever quantity.

The term “and/or” placed between a first entity and a second entityincludes any of the meanings of (1) only the first entity, (2) only thesecond entity, and (3) the first entity and the second entity. The term“and/or” placed between the last two entities of a list of 3 or moreentities means at least one of the entities in the list including anyspecific combination of entities in this list. For example, “A, B and/orC” has the same meaning as “A and/or B and/or C” and comprises thefollowing combinations of A, B and C: (1) only A, (2) only B, (3) onlyC, (4) A and B and not C, (5) A and C and not B (6) B and C and not A,and (7) A and B and C.

The phrase “at least one of” preceding a list of features or entitiesmeans one or more of the features or entities in the list of entities,but not necessarily including at least one of each and every entityspecifically listed within the list of entities and not excluding anycombinations of entities in the list of entities. For example, “at leastone of A, B, or C” (or equivalently “at least one of A, B, and C” orequivalently “at least one of A, B, and/or C”) has the same meaning as“A and/or B and/or C” and comprises the following combinations of A, Band C: (1) only A, (2) only B, (3) only C, (4) A and B and not C, (5) Aand C and not B, (6) B and C and not A, and (7) A and B and C.

The phrase “at least a portion” means “a portion or all.” “At least aportion” of a stream may have the same composition with the sameconcentration of each of the species as the stream from which it isderived, a different concentration of species than that of the streamfrom which it is derived, or may include only specific species of thestream from which it is derived.

As used herein a “divided portion” of a stream is a portion having thesame chemical composition and species concentrations as the stream fromwhich it was taken.

The term “depleted” means having a lesser mole % concentration of theindicated component than the original stream from which it was formed.“Depleted” does not mean that the stream is completely lacking theindicated component.

The terms “rich” or “enriched” means having a greater mole %concentration of the indicated component than the original stream fromwhich it was formed.

As used herein, “first,” “second,” “third,” etc. are used to distinguishfrom among a plurality of steps and/or features, and are not indicativeof the total number, or relative position in time and/or space unlessexpressly stated as such.

To aid in describing the invention, directional terms may be used in thespecification and claims to describe portions of the present invention(e.g., upper, lower, left, right, etc.). These directional terms aremerely intended to assist in describing and claiming the invention andare not intended to limit the invention in any way. In addition,reference numerals that are introduced in the specification inassociation with a drawing figure may be repeated in one or moresubsequent figures without additional description in the specificationin order to provide context for other features.

In the claims, letters may be used to identify claimed steps (e.g. (a),(b), and (c)). These letters are used to aid in referring to the methodsteps and are not intended to indicate the order in which claimed stepsare performed, unless and only to the extent that such order isspecifically recited in the claims.

In certain embodiments, the present invention provides systems andmethods for recovering helium from a feed stream comprising helium,carbon dioxide (CO₂), and one or more components of intermediatevolatility (i.e. having a volatility between those of helium and CO₂).Such components are referred to herein as “intermediate components,” andmay include (but are not limited to) nitrogen, hydrogen, argon, methane,and ethane. The methods comprise separating CO₂ and intermediatecomponents from helium at a temperature greater than −82.7° C., oralternatively at a temperature greater than −56.6° C., and forming ahelium-rich product stream, wherein the concentration of at least one ofthe intermediate components in the helium-rich product stream is lowerthan its concentration in the feed stream. In one or more embodiments ofthe methods of the present invention, at least part of the separation iseffected by contacting a vapor with a liquid. In one or moreembodiments, at least part of the method takes place at a temperaturebelow the ambient temperature.

In certain embodiments, the feed stream may comprise at least 50 mol %CO₂, or at least 60 mol % CO₂, or at least 70 mol % CO₂, or at least 75mol % CO₂, or at least 80 mol % CO₂, or at least 85 mol % CO₂, or atleast 90 mol % CO₂. Further, the feed streams employed in the presentinvention generally comprise less than about 3 mol %, or less than about2 mol %, or less than about 1 mol % helium, and may comprise from 0 toabout 15 mol %, or from 1 to about 10 mol %, or from 2 to about 8 mol %nitrogen. The feed stream may be a gas, liquid, or mixed feed, and mayoptionally comprise a supercritical fluid. In one or more embodiments, ahigh pressure feed may be employed; for example, the pressure of thefeed stream may be greater than about 30 bar, or greater than about 35bar, or greater than about 40 bar.

In some embodiments, systems and methods of the present inventionfurther comprise the steps of cooling the feed stream, and separatingthe feed stream in a first separator to form a first helium-enrichedstream and a first CO₂-enriched stream. The streams may be cooled andseparated by any available means known to those skilled in the art andcompatible with the overall process and desired results. For example,the streams may be cooled, and other streams in the process heated, in asingle heat exchanger that provides thermal control and integration forthe process as a whole. Alternately, multiple heat exchangers, one ormore refrigeration units or chillers, or other cooling methods may beused. The feed stream may optionally be dried prior to cooling to removeenough water from the feed to avoid formation of ice or CO₂ hydrate inthe process. For example, the feed stream may be dried to achieve awater dew point less than or equal to −40° C. The feed stream may bedried using any suitable drying process or equipment. For example, thefeed stream may be dried via temperature swing adsorption.

Similarly, the streams may be separated by any available means known tothose skilled in the art and compatible with the overall process anddesired results. Although the term “separator” is predominantly usedherein for ease of reference, the term is intended to encompass anysuitable separation device or devices. For example, the feed stream maybe separated using one or more packed or trayed columns, one or moreflash separators, one or more adsorption units, membrane separators,etc. Preferably, the feed stream is separated via a distillation columnand the first helium-enriched stream is optionally separated via anadsorption unit such as a pressure swing adsorption system (PSA).

The distillation column may optionally include one or more reboilers, inwhich a liquid stream is withdrawn from the column, heated and at leastpartially vaporized, and at least the vapor portion is returned to thecolumn. The one or more reboilers may vaporize liquid withdrawn from thebottom of the column or from an intermediate stage of the column, andmay similarly return vapor to the bottom of the column or to anintermediate stage of the column. In one or more embodiments of theinvention, the distillation column comprises a bottom reboiler. Infurther embodiments, the distillation column comprises a bottom reboilerand one or more intermediate reboilers.

In some embodiments of the present invention, the distillation columnmay incorporate a “CO₂ wash,” in which the feed stream enters the columnat an intermediate stage and a liquid stream comprising CO₂ (generallyin addition to other components) is fed to the top of the column.

In this manner, nitrogen is washed from the helium-enriched overheadstream of the column and moved to the first CO₂-enriched stream. The CO₂wash also has the benefit of removing methane and other hydrocarbonsfrom the overhead stream, eliminating impurities that would otherwisehave to be removed in a subsequent cryogenic purification process. As aresult, the use of a CO₂ wash in the distillation column results in ahigher overall helium recovery when compared to a column without a CO₂wash stream. For example, the helium-rich product stream generated bythe systems and methods of the present invention will generally compriseat least about 60 mol % helium when the distillation column is operatedwithout a CO₂ wash. When a CO₂ wash is employed in the distillationcolumn, however, the helium-rich product stream may comprise greaterthan 85 mol % helium, or greater than 90 mol % helium, or greater than92 mol % helium, or greater than 95 mol % helium.

The CO₂ wash may come from a variety of sources. For example, in certainembodiments of the invention, the first CO₂-enriched stream exiting thedistillation column may be split into two or more derivativeCO₂-enriched streams. One or more of the derivative CO₂-enriched streamsmay then be separated into a vapor fraction and a liquid fraction, andthe liquid fraction obtained as a result may be recycled to the top ofthe column as a CO₂ wash stream. In such methods, the derivativeCO₂-enriched stream may optionally be heated prior to separation, andthe liquid fraction may optionally be cooled before being fed to the topof the distillation column. In other embodiments, the CO₂ wash streammay be taken from the feed stream. In such embodiments, the feed streamis partially cooled and separated into a liquid fraction and a vaporfraction. At least a portion of the liquid fraction is directed to thetop of the distillation column, while the vapor fraction is furthercooled and fed to the distillation column. Optionally, the at least aportion of the liquid fraction may be further cooled prior to enteringthe top of the distillation column. Persons of skill in the art willrecognize that CO₂ wash streams may come from a variety of sourceswithin the processes described herein, provided that they comprise asufficient amount of CO₂ to be effective for the intended purpose. CO₂wash streams from any such source are contemplated herein and are withinthe scope of the present invention.

Some systems and methods of the present invention further comprise thesteps of splitting the first CO₂-enriched stream into two or morederivative CO₂-enriched streams, heating at least one of the derivativeCO₂-enriched streams (for example via a heat exchanger also used to coolthe feed stream), and combining the two or more derivative CO₂-enrichedstreams to form a CO₂-rich product stream. One or more of the streamsmay optionally be compressed before the streams are combined.

Some systems and methods of the present invention further comprise theelimination (or rejection) of at east one of the components ofintermediate volatility. Such systems and methods further compriseseparating one of the derivative CO₂-enriched streams in a secondseparator into a liquid fraction and a vapor fraction, cooling the vaporfraction, and separating the resulting cooled fraction into (i) aproduct stream enriched in at least one of the components ofintermediate volatility and (ii) a CO₂-rich recycle stream. Optionally,the liquid fraction exiting the second separator may be heated andfurther separated in to a secondary liquid fraction and a secondaryvapor fraction, and the secondary liquid fraction may be recycled to thetop of the distillation column to provide a CO₂ wash. In one or moreembodiments, the second separator is a distillation column. In the sameor other embodiments, the product stream enriched in at least one of thecomponents of intermediate volatility comprises nitrogen. Preferably,the product stream is nitrogen-rich. In such systems and methodsincorporating nitrogen rejection, the CO₂-rich recycle stream may berecombined with the first CO₂-enriched stream exiting the distillationcolumn (or recombined with one of the derivative CO₂-enriched streamsformed after the CO₂-rich recycle stream is split), thus forming part ofthe CO₂-rich product stream. The CO₂-rich product stream in suchembodiments may comprise greater than 80 mol % CO₂, or greater than 85mol % CO₂, or greater than 90 mol % CO₂, or greater than 95 mol % CO₂.

In some embodiments, the first helium-enriched stream is separated in athird separator to form the helium-rich product stream and a helium-leanstream. Preferably, the first helium-enriched stream is separated in aPSA. The PSA may be configured to remove, for example, nitrogen, argon,and CO₂ from the first helium-enriched stream. The helium-lean streammay then be directed downstream for further processing, removed as aproduct, or recycled. If recycled, the helium-lean stream may beindependently fed to the distillation column, or may alternatively becombined with the feed stream at a point upstream of the distillationcolumn.

In the same or other systems and methods of the invention, the firsthelium-enriched stream exiting the distillation column may comprise oneor more combustible components. In such embodiments, the combustiblecomponents of the first helium-enriched stream may be catalyticallycombusted in the presence of oxygen to at least partially convert thecombustible components (such as, for example, hydrogen and/or methane)into CO₂ and water. The water may then be removed, either in a separatestep or when the first helium-enriched stream is separated to form thehelium-rich product stream and the second CO₂-enriched stream. Bycombusting the first helium-enriched stream in this manner and removingat least a portion of the combustion products, a substantially purehelium product stream may be obtained. For example, the helium-richproduct stream may comprise at least 98 mol % helium, or at least 99 mol% helium, or at least 99.5 mol % helium, or at least 99.9 mol % helium.In systems and methods incorporating both nitrogen rejection andcombustion of the first helium-enriched stream, a CO₂ composition in theCO₂-rich product stream can be obtained such that the CO₂-rich productstream meets downstream pipeline requirements while also achieving asubstantially pure helium product. For example, the CO₂-rich productstream may comprise greater than 90 mol % CO₂, or greater than 92 mol %CO₂, or greater than 95 mol % CO₂. Alternatively, or in addition tocatalytic combustion, hydrogen may be removed by oxidation with aninorganic oxide, such as in beds provided in tandem for switchingbetween on-line and regeneration modes. Suitable inorganic oxidesinclude, but are not limited to, copper (II) oxide (CuO).

In certain embodiments of the invention, it may be unnecessary orundesirable to further separate or purify the first helium-enrichedstream downstream of the distillation column. In such embodiments, thePSA described above may be eliminated, while the remainder of theprocess remains unchanged and may have any of the configurations or acombination of the configurations described herein. For example,configurations that include a CO₂ wash stream in the distillation columnmay be adapted to operate without the PSA, regardless of the source ofthe CO₂ wash stream and regardless of whether the configuration alsoincorporates nitrogen rejection.

Having described the various aspects of the compositions herein, furtherspecific embodiments of the invention include those set forth in thefollowing lettered paragraphs:

A. A method for recovering helium from a feed stream comprising helium,carbon dioxide, and one or more intermediate components havingvolatilities between those of carbon dioxide and helium, the methodcomprising separating the carbon dioxide and the intermediate componentsfrom the helium at a temperature greater than −82.7° C. to form ahelium-rich product stream, wherein the concentration of at least one ofthe intermediate components in the helium-rich product stream is lowerthan its concentration in the feed stream, and wherein at least part ofthe separation is effected by contacting a vapor with a liquid.

B. The method of paragraph A, wherein the carbon dioxide and theintermediate components are separated from the helium at a temperaturegreater than −56.6° C.

C. The method of any of paragraphs A through B, wherein the feed streamcomprises at least 50 mol % carbon dioxide.

D. The method of any of paragraphs A through C, wherein at least part ofthe method takes place at a temperature below the ambient temperature.

E. The method of any of paragraphs A through D, further comprising thesteps of:

(a) cooling the feed stream; (b) separating the feed stream into a firsthelium-enriched stream and a first CO₂-enriched stream; and (c)separating the first helium-enriched stream to form the helium-richproduct stream and a helium-lean stream.

F. The method of paragraph E, further comprising the steps of: (d)splitting the first CO₂-enriched stream into two or more derivativeCO₂-enriched streams; (e) heating at least one of the two or morederivative CO₂-enriched streams; and (f) compressing and combining thetwo or more derivative CO₂-enriched streams to form a CO₂-rich productstream.

G. The method of any of paragraphs E through F, wherein the feed streamis dried to a water dew point of less than or equal to −40° C. prior tocooling the feed stream.

H. The method of any of paragraphs E through G, wherein the feed streamis separated in step b) in a distillation column and wherein thehelium-lean stream is recycled and fed to the distillation column.

I. The method of paragraph H, wherein the recycled helium-lean stream iscombined with the feed stream before being fed to the distillationcolumn.

J. The method of any of paragraphs E through I, wherein the feed streamis separated in step b) in a distillation column having a firstreboiler, wherein a first liquid stream is withdrawn from the bottom ofthe distillation column, heated and at least partially vaporized, and atleast the vapor portion of the heated first liquid stream is returned tothe bottom of the distillation column.

K. The method of paragraph J, wherein the distillation column furthercomprises a second reboiler, wherein a second liquid stream is withdrawnfrom an intermediate stage of the distillation column, heated and atleast partially vaporized, and at least the vapor portion of the heatedsecond liquid stream is returned to an intermediate stage of thedistillation column.

L. The method of any of paragraphs J through K, wherein at least part ofthe feed stream enters the distillation column at an intermediatelocation, further comprising feeding a liquid stream comprising CO₂ tothe top of the distillation column.

M. The method of any of paragraphs F through I, wherein the feed streamis separated in step b) in a distillation column and at least part ofthe feed stream enters the distillation column at an intermediatelocation, further comprising separating at least one of the two or morederivative CO₂-enriched streams into a liquid fraction and a vaporfraction and feeding the liquid fraction to the top of the distillationcolumn.

N. The method of paragraph M, wherein the derivative CO₂-enriched streamis heated prior to separating the stream into the liquid fraction andthe vapor fraction and wherein the liquid fraction is cooled prior toentering the top of the distillation column.

O. The method of paragraph L or M, wherein the helium-rich productstream comprises at least 90 mol % helium.

P. The method of any of paragraphs F through O, further comprisingseparating one of the derivative CO₂-enriched streams into a liquidfraction and a vapor fraction, cooling the vapor fraction of thederivative CO₂-enriched stream, and separating the resulting cooledfraction into a product stream enriched in at least one of thecomponents of intermediate volatility and a CO₂-rich recycle stream.

Q. The method of any of paragraphs F through O, further comprisingseparating one of the derivative CO₂-enriched streams into a liquidfraction and a vapor fraction, cooling the vapor fraction, andseparating the resulting cooled fraction into a nitrogen-rich productstream and a CO₂-rich recycle stream.

R. The method of any of paragraphs E through Q, wherein the firsthelium-enriched stream comprises one or more combustible components,further comprising catalytically combusting the combustible componentsof the first helium-enriched stream in the presence of oxygen to atleast partially convert the combustible components to CO₂ and water andremoving the water prior to or in the same step as separating the firsthelium-enriched stream to form the helium-rich product stream and thesecond CO₂-enriched stream.

S. The method of paragraph R, wherein the helium-rich product streamcomprises at least 99 mol % helium.

T. The method of any of paragraphs A through R, wherein the helium-richproduct stream comprises at least 60 mol % helium.

U. The method of any of paragraphs F through T, wherein the CO₂-richproduct stream comprises at least 90 mol % CO₂.

V. The method of any of paragraphs F through U, wherein the CO₂-richproduct stream comprises at least 95 mol % CO₂.

W. The method of any of paragraphs A through V, wherein the feed streamcomprises a gas.

X. The method of any of paragraphs A through W, wherein the feed streamcomprises a liquid.

Y. The method of any of paragraphs A through X wherein the feed streamcomprises a supercritical fluid.

Z. The method of any of paragraphs A through Y, wherein the pressure ofthe feed stream is greater than about 35 bar.

AA. A system for recovering helium from a feed stream, the systemcomprising: (a) a feed stream comprising helium and at least 50 mol %CO₂; (b) a first separator comprising a distillation column configuredto separate the feed stream into a first helium-enriched stream and afirst CO₂-enriched stream, wherein at least part of the feed streamenters the distillation column at an intermediate location; (c) one ormore heat exchangers configured to cool the feed stream and heat thefirst helium-enriched and first CO₂-enriched streams; (d) a secondseparator configured to separate (i) the feed stream and/or (ii) aportion of the first CO₂-enriched stream into a liquid fraction and avapor fraction and recycle the liquid fraction to the top of thedistillation column; and (e) a compressor configured to compress thenon-separated portion of the first CO₂-enriched stream and the vaporfraction of any separated portion of the first CO₂-enriched stream toform a CO₂-rich product stream.

BB. The system of paragraph AA, further comprising a third separatorconfigured to separate the first helium-enriched stream to form ahelium-rich product stream and a helium-lean stream.

CC. The system of any of paragraphs AA through BB, further comprising adrier configured to dry the feed stream to a water dew point of lessthan or equal to −40° C. before the feed stream is cooled in the heatexchanger.

DD. The system of any of paragraphs BB through CC, wherein thehelium-lean stream is recycled and fed to the distillation column.

EE. The system of any of paragraphs AA through DD, wherein the firstseparator further comprises a first reboiler configured to supply vaporto the bottom of the distillation column.

FF. The system of paragraph EE, wherein the first separator furthercomprises a second reboiler configured to supply vapor to anintermediate stage of the distillation column.

GG. The system of any of paragraphs AA through FF, wherein the feedstream or the portion of the first CO₂-enriched stream s heated prior toentering the second separator and the liquid fraction is cooled prior toentering the top of the distillation column.

HH. The system of any of paragraphs BB through GG, wherein thehelium-rich product stream comprises at least 90 mol % helium.

II. The system of any of paragraphs BB through HH, wherein the thirdseparator comprises a pressure swing adsorption unit (PSA).

JJ. The system of paragraph II, wherein the PSA is configured to removeat least nitrogen, argon, and CO₂ from the first helium-enriched stream.

KK. The system of any of paragraphs AA through JJ, further comprising afourth separator, wherein the vapor fraction exiting the secondseparator is cooled and wherein the fourth separator is configured toseparate the resulting cooled fraction into a CO₂-rich recycle streamand a product stream rich in one or more intermediate components havinga volatility between those of CO₂ and helium.

LL. The system of paragraph KK, wherein in step d) the liquid fractionexiting the second separator is heated and separated into a secondaryliquid fraction and a secondary vapor fraction and the secondary liquidfraction is recycled to the top of the distillation column.

MM. The system of any of paragraphs AA through LL, wherein the secondseparator is a distillation column.

NN. The system of any of paragraphs KK through MM, wherein the fourthseparator is a distillation column.

OO. The system of any of paragraphs BB through NN, wherein the firsthelium-enriched stream comprises one or more combustible components,further comprising a catalytic combustor configured to combust the firsthelium-enriched stream in the presence of oxygen to at least partiallyconvert the combustible components to CO₂ and water and optionallyremove at least part of the water before the first helium-enrichedstream enters the second separator.

PP. The system of paragraph OO, wherein the helium-rich product streamcomprises at least 99 mol % helium.

QQ. The system of any of paragraphs AA through OO, wherein thehelium-rich product stream comprises at least 60 mol % helium.

RR. The system of any of paragraphs BB through QQ, wherein the CO₂-richproduct stream comprises at least 90 mol % CO₂.

SS. The system of any of paragraphs BB through RR, wherein the CO₂-richproduct stream comprises at least 95 mol % CO₂.

TT. The system of any of paragraphs AA through SS, wherein the feedstream comprises a gas.

UU. The system of any of paragraphs AA through TT, wherein the feedstream comprises a liquid.

VV. The system of any of paragraphs AA through UU, wherein the feedstream comprises a supercritical fluid.

WW The system of any of paragraphs AA through VV, wherein the pressureof the feed stream is greater than about 35 bar.

A1. A method for recovering helium from a feed stream containing helium,carbon dioxide and at least one of methane and nitrogen, the methodcomprising:

-   -   introducing a separator feed stream into a separator, the        separator feed stream comprising at least a portion of the feed        stream, separating the separator feed stream into a first        helium-enriched stream and a first CO₂-enriched stream, and        withdrawing the first helium-enriched stream and the first        CO₂-enriched stream from the separator;    -   introducing a pressure swing adsorption unit feed stream into a        pressure swing adsorption unit, the pressure swing adsorption        unit feed stream comprising at least a portion of the first        helium-enriched stream, separating the pressure swing adsorption        unit feed stream into a helium-rich product stream and a        helium-lean stream, and withdrawing the helium-rich product        stream and the helium-lean stream from the pressure swing        adsorption unit;    -   compressing a compressor feed stream in a compressor to form a        compressor effluent stream, the compressor feed stream        comprising the helium-lean stream and a helium-enriched permeate        stream;    -   introducing a first portion of the compressor effluent stream        into a membrane separation unit, separating the first portion of        the compressor effluent stream to form the helium-enriched        permeate stream and a helium-depleted non-permeate stream, and        withdrawing the helium-enriched permeate stream and the        helium-depleted non-permeate stream from the membrane separation        unit; and    -   introducing a second portion of the compressor effluent stream        into the separator.

A2. The method of paragraph A1 wherein the second portion of thecompressor effluent stream is introduced into the separator as part ofthe separator feed stream, the separator feed stream comprising the atleast a portion of the feed stream and the second portion of thecompressor effluent stream.

A3. The method of paragraph A1 wherein the second portion of thecompressor effluent stream is introduced into the separator separatelyfrom the separator feed stream comprising the at least a portion of thefeed stream.

A4. The method of any one of paragraphs A1 to A3 wherein the firstportion of the compressor effluent stream has a molar flow rate, F₁, thesecond portion of the compressor effluent stream has a molar flow rate,F₂, and wherein 0.60≦F₁/F₂≦0.85.

A5. The method of any one of paragraphs A1 to A4 wherein the membraneseparation unit comprises a separation module wherein the separationmodule is a hollow fiber module or a spiral wound module.

A6. The method of paragraph A5 wherein the separation module comprises amembrane, wherein the membrane comprises a support, wherein the supportcomprises a material selected from the group consisting of polysulfone,cellulose acetate, an aromatic polyimide, an aromatic polyamide, anaromatic polycarbonate, poly(dimethyl phenylene oxide), poly(dimethylsiloxane), and carbon molecular sieve.

A7. The method of paragraph A5 or paragraph A6 wherein the separationmembrane is a mixed matrix membrane.

A8. The method of paragraph A5 or paragraph A6 wherein the separationmembrane is a facilitated transport membrane.

A9. The method of any one of paragraphs A1 to A8 wherein the separatoris a pressure swing adsorption separator.

A10. The method of any one of paragraphs A1 to A9 wherein the separatoris a fractionator.

A11. The method of paragraph A10, wherein the fractionator is adistillation column, wherein the first helium-enriched stream iswithdrawn from an upper location of the distillation column, and thefirst CO₂-enriched stream is withdrawn from a lower location of thedistillation column, the method further comprising the steps of:

-   -   cooling the feed stream to form the separator feed stream; and    -   feeding a liquid stream comprising CO₂ to an upper portion of        the distillation column as a CO₂ wash stream;    -   wherein at least part of the separator feed stream is introduced        into the distillation column at an location intermediate the        upper location of the distillation column and the lower location        of the distillation column.

A12. The method of any one paragraphs A1 to A11 wherein the feed streamhas a CO₂ concentration of at least 50 mole % CO₂.

A13. The method of any one of paragraphs A1 to A12, wherein the firsthelium-enriched stream comprises one or more combustible components, themethod further comprising catalytically combusting the combustiblecomponents in the first helium-enriched stream in the presence of oxygento at least partially convert the combustible components to CO₂ and H₂Othereby forming a combustible component-depleted helium-enriched streamwherein the pressure swing adsorption unit feed stream comprises thecombustible component-depleted helium-enriched stream as the at least aportion of the first helium-enriched stream.

A14. A system for recovering helium from a feed stream containinghelium, carbon dioxide and at least one of methane and nitrogen, thesystem comprising:

-   -   a separator operatively disposed to receive a separator feed        stream, the separator feed stream comprising at least a portion        of the feed stream, the separator operatively configured to        separate the separator feed stream into a first helium-enriched        stream and a first CO₂-enriched stream;    -   a pressure swing adsorption unit operatively configured to        separate a pressure swing adsorption unit feed stream into a        helium-rich product stream and a helium-lean stream, the        pressure swing adsorption unit feed stream comprising at least a        portion of the first helium-enriched stream;    -   a compressor operatively disposed to receive a compressor feed        stream comprising the helium-lean stream and a helium-enriched        permeate stream, the compressor operatively configured to        compress the compressor feed stream to form a compressor        effluent stream; and    -   a membrane separation unit operatively disposed to receive a        first portion of the compressor effluent stream and operatively        configured to separate the first portion of the compressor        effluent stream into the helium-enriched permeate stream and a        helium-depleted non-permeate stream;    -   wherein the separator is also operatively disposed to receive a        second portion of the compressor effluent stream.

A15. The system of paragraph A14 wherein the membrane separation unitcomprises a separation membrane wherein the separation membrane is ahollow fiber membrane or a spiral wound membrane.

A16. The system of paragraph A15 wherein the separation membranecomprises a support, wherein the support comprises a material selectedfrom the group consisting of polysulfone, cellulose acetate, an aromaticpolyimide, an aromatic polyamide, an aromatic polycarbonate,poly(dimethyl phenylene oxide), poly(dimethyl siloxane), and carbon.

A17. The system of paragraph A15 or paragraph A16 wherein the separationmembrane is a mixed matrix membrane.

A18. The system of paragraph A15 or paragraph A16 wherein the separationmembrane is a facilitated transport membrane.

A19. The system of any one of paragraphs A14 to A18 wherein theseparator is a pressure swing adsorption separator.

A20. The system of any one of paragraphs A14 to A18 wherein theseparator is a fractionator.

A21. The system of paragraph A20 wherein the fractionator is adistillation column,

-   -   wherein the distillation column has a first outlet operatively        disposed to withdraw the first helium-enriched stream, the first        outlet located in an upper portion of the distillation column;    -   wherein the distillation column has a second outlet operatively        disposed to withdraw the first CO₂-enriched stream, the second        outlet located in a lower portion of the distillation column;    -   wherein the distillation column has a first inlet operatively        disposed to introduce the separator feed stream, the first inlet        located at a position intermediate the upper portion of the        distillation column and the lower portion of the distillation        column;    -   wherein the distillation column has a second inlet operatively        disposed to introduce a CO₂ wash stream, the second inlet        located in the upper portion of the distillation column;        the system further comprising:    -   one or more heat exchangers operatively configured to cool the        at least a portion of the feed stream to form the separator feed        stream by indirect heat transfer with a portion or all of the        first helium-enriched stream and a portion or all of the first        CO₂-enriched stream thereby heating the portion or all of the        first helium-enriched stream and the portion or all of the first        CO₂-enriched stream.

A22. The system of any one of paragraphs A14 to A21, wherein the firsthelium-enriched stream comprises one or more combustible components, thesystem further comprising a catalytic combustor (containing a catalyst)operatively configured to combust the one or more combustible componentsin the first helium-enriched stream in the presence of oxygen to atleast partially convert the combustible components to CO₂ and H₂Othereby forming a combustible component-depleted helium-enriched streamwherein the pressure swing adsorption unit feed stream comprises thecombustible component-depleted helium-enriched stream as the at least aportion of the first helium-enriched stream.

A23. The system of any one of paragraphs A14 to A22 wherein the feedstream has a CO₂ concentration of at least 50 mole % CO₂.

DETAILED DESCRIPTION OF THE DRAWINGS AND EXAMPLES

The systems and methods of the invention may be further understood withreference to FIGS. 1 through 9 and the descriptions thereof that follow.It should be noted that the figures are simplified flow diagrams and, insome instances, do not show various pieces of auxiliary equipment, suchas pumps, compressors, heat exchangers, and valves. Because one havingordinary skill in the art would recognize easily the need for andlocation of such auxiliary equipment, its omission is appropriate andfacilitates the simplification of the figures. Fluid streams andequipment common to more than one figure or embodiment are identified bythe same reference numerals in each figure. In the interest of clarity,some of these shared features that are described with respect to thefigure in which they first appear are numbered in subsequent figures butthose descriptions are not repeated in the specification.

In the examples that accompany the discussion of the figures, two feedgas compositions are used, referred to as a Low N₂ Feed and a High N₂Feed. These compositions are shown in Table 1 on a dry basis, i.e.excluding any water that may be present. The compositions are given on amolar basis in Table 1 and throughout the discussion that follows. Thesetwo compositions were chosen to exemplify the invention because they areconsidered to be typical of a helium-containing CO₂ field with low andhigh levels of nitrogen. Those skilled in the art, however, willrecognize that the systems and methods of the present invention aredesigned to recover helium from feed streams having a wide variety ofcompositions, and all such possible feed compositions are contemplatedherein.

TABLE 1 Component Low N₂ Feed High N₂ Feed CO₂, mol % 96.38 92.38 N₂,mol % 3.00 7.00 He, mol % 0.35 0.35 CH₄, mol % 0.20 0.20 H₂, ppm 100 100Ar, ppm 600 600 C₂H₆, ppm 1 1 H₂S, ppm 5 5

The High N₂ Feed composition shown in Table 1 is particularlysignificant, in that the CO₂ content is less than a typical pipelinerequirement of 95%. The present invention provides the ability recoverhelium from the feed while simultaneously increasing the CO₂concentration to the 95% level required by the pipeline. In the case ofboth the Low N₂ Feed and the High N₂ Feed, the amount of helium in thefeed stream was maintained at a constant value of 30.72 kmol/hr toensure a consistent basis for comparison. The feed CO₂ is at a pressureof 705 psi (48.6 bar), and all of the exemplary processes describedbelow compress the product CO₂ to the same pressure as the feed.

All of the processes described herein were modeled using thecommercially available software package Aspen Plus V7.2 produced byAspen Technology, Inc. This program was used to model the physicalprocesses, and its optimizer was used to determine the optimum operatingparameters, including pressures and flow rates.

FIG. 1 shows an exemplary system for recovering helium from aCO₂-containing feed. FIG. 1 and its accompanying description areincluded to provide necessary background information for subsequentFigures depicting embodiments of the invention and to establish thestate of the art. The feed stream S100 has the composition shown inTable 1. A process in which the feed stream S100 has the Low N₂ Feedcomposition will be considered first. In this low N₂ example, streamS100 is at 705 psi (48.6 bar) and is dried in a drier A101 (such as atemperature swing adsorption (TSA) unit, pressure swing adsorption (PSA)unit, or glycol drier) to remove water via stream S101, leaving streamS102 essentially water-free. In practice, there will be some water leftin stream S102, for example up to about 50 ppm, but sufficient water isremoved in drier A101 to prevent problems that would be caused by waterfreezing or forming solid CO₂ hydrates in the subsequent low temperatureprocess. The drier A101 will therefore dry the feed stream S100 to belowa water dew point of approximately −40° C.

The dried stream S102 is then mixed with compressed recycled gas instream S123 to form stream S103 and cooled to −49° C. in heat exchangerHX100 to yield stream S104, which causes most of the CO₂ in the driedfeed stream S102 to condense. The condensed CO₂-rich liquid phase ofstream S104, which is 97.2% of the total flow, is then separated fromthe vapor phase of S104 in phase separator C100, resulting in a firstCO₂-enriched liquid stream S105 and a helium-enriched vapor stream S106.Stream S106 comprises 2.8% of the stream fed to HX100 through streamS103. This vapor stream has been enriched in helium due to thecondensing of the predominant CO₂ component from the gas phase and has aconcentration of 13.3% helium.

The helium-enriched stream S106 is then re-heated in HX100 and passed toa PSA unit A100. The warmed, helium-enriched stream S107 still containssome CO₂, in this case 21.1% CO₂; and the PSA A100 is used to remove theresidual CO₂ as the CO₂ is an impurity that could freeze and blockequipment during subsequent low temperature purification of the crudehelium. The PSA A100 will prevent substantially all of the CO₂ in streamS107 from reaching the crude helium-rich product stream S108 byrejecting the CO₂ into helium-lean stream S109. The crude helium-richproduct stream S108 is purified by the PSA process in A100 to produce acomposition of 547% nitrogen, 42.8% helium, 0.6% methane, 1.1% hydrogen,and 0.85% argon, with less than 1 ppm C₂H₆ and H₂S, and up to about 1ppm CO₂. The rest of stream S107 fed to the PSA A100 is recovered to theprocess in helium-lean stream S109. Stream S109 has the composition ofthe stream that is recovered from the adsorbent in the PSA A100 when itis regenerated by reducing the pressure of the bed, releasing thecomponents that make up stream S109. Helium-lean stream S109 istherefore at low pressure (1.6 bar) and must be recompressed in one ormore compressors K101 and K102 to recover the stream to the feed. It isimportant that this stream is recovered to the process, as it contains15% of the helium that was fed to PSA A100. Additionally, the CO₂ inthis stream S109 is also recovered.

There is still significant helium in the CO₂-enriched liquid stream S105exiting the first separator C100. In fact, about 21% of the helium instream S104 leaves C100 in the liquid stream S105. In order to maximizethe recovery of helium from the feed stream S100, this helium can bestripped from the liquid by reducing the pressure and recovering thevapor, which is then recompressed and recycled to the feed. In FIG. 1,this is shown by stream S105 returning to heat exchanger HX100, where itis warmed to −45° C. This heating forms a significant part of thecooling required for HX100 to condense the liquid phase separated inC100.

The warmed CO₂-enriched stream S111 is then reduced in pressure to about25 bar through valve V100 to form stream S112. Only about 2% of thehelium fed in feed stream S100 remains in liquid CO₂ stream S115, whichresults from separation of stream S112 in phase separator C101. Thisexemplary process was optimized to give 98% helium recovery; reducingthe pressure further through V100 would allow for increased heliumrecovery; however such higher helium recovery would be at the expense ofhigher recompression power. The vapor stream S113 exiting phaseseparator C101 contains the recovered helium and is warmed in HX100 togive warmed stream 3114, which is then recompressed in compressor K102to the feed pressure and mixed with the dried feed stream S102 toproduce stream S103.

The refrigeration required to condense the feed stream S100 is providedpartly by the warming of stream S105, but most of the refrigerationcomes from reheating helium-lean liquid CO₂ stream S115, which exitsphase separator C101. Stream S115 is split into a number of derivativestreams. (Two derivative streams S116 and 3117 are shown in FIG. 1, butstream S115 may be split into any number of derivative streams to suitthe requirements of a particular process.) The derivative streams S116and S117 are warmed in HX100. These derivative streams may be adjustedin pressure via a valve (such as V101) or a pump (such as P100) toprovide refrigeration at different pressure, and therefore temperature,levels. The split between these streams and the pressure to which theyare reduced, or pumped, may be easily determined by those skilled in theart so as to optimize the process.

In the system depicted in FIG. 1, some of liquid stream S115 is splitinto stream S116 and dropped in pressure through valve V101 to about 7.8bar, so that it boils at a cold enough temperature to provide sufficienttemperature difference at the cold end of the heat exchanger. Theresulting stream S118 exiting valve V101 is the coldest part of theprocess, and the optimization used herein has constrained thetemperature of stream S118 to be greater than the freezing point of CO₂(and so is at an imposed lower limit of −56° C.). This stream S118 isonly a small amount of stream S115, about 5.8%, and serves to open theheat exchanger cooling curve at the cold end. The rest of stream S115,split into stream S117, is pressurized to about 36 bar with pump P100 toresult in stream S119, as the pressure required for the stream to boilat the optimal conditions is higher than the pressure required in C101to drive off the rest of the helium. This pressure was determined by thedesired recovery of helium in the process. Part of stream S115 may alsobe split into an additional stream (not shown) at a third pressure tofurther optimize the performance of heat exchanger HX100, therebyreducing the subsequent power for recompression, but this was notrequired in this example. Much of the refrigeration in this process alsocomes from the re-warming of the CO₂-enriched liquid stream S105.

Compressors are used in the process shown in FIG. 1, first to recompressthe recycled streams S114 and S109, second to compress the low pressurewarmed CO₂ stream S120 (which results from warming stream S118 in heatexchanger HX100) to the pressure of the CO₂ after pump P100, and finallyfor compression to the product pressure (these two stages of compressionare shown as one compressor K100 with an intermediate feed stream S121,which results from warming stream S119 in heat exchanger HX100, in FIG.1).

The products from the process are the CO₂-rich product stream S122,which contains substantially all of the CO₂ from feed stream S100, and acrude helium-rich product stream S108 that can be further purified andliquefied to produce a pure helium stream. The performance of the doubleflash cycle process depicted in FIG. 1 is summarized in Table 2.

The double flash cycle of FIG. 1 with the High N₂ Feed composition givenin Table 1 is now considered. The performance of this example is alsoshown in Table 2. The main differences with this higher nitrogen feedare as follows. Because more helium is recovered in the first separatorC100, the pressure of the second separator C101 does not need to be solow, i.e. about 40 bar compared with about 25 bar. The higher pressureCO₂ stream S109 used for refrigeration is still around the same pressure(about 36 bar compared to about 33 bar), so in this case P100 would bereplaced with a pressure reduction valve. The higher amount of nitrogenin the feed leads to a lower first enriched helium composition in streamS106 exiting separator C100, of 3.55% compared with 13.27%. This alsoleads to a product crude helium stream S108 of lower helium composition,14.76% vs. 42.77%, since the performance of the PSA A100, i.e. therecovery of components to the product stream, is assumed to be constant.Further, the extra nitrogen carried through to the PSA A100 means thatthe PSA A100 will be larger. Finally, the most significant differencebetween the low N₂ feed and the high N₂ feed scenarios is the increasein power consumption, particularly the recompression power, which ismostly the extra power required to recompress the increased CO₂ andnitrogen rejected in stream S109 from the PSA A100, due to the increasedamounts of these components in the vapor from stream S106.

As shown in Table 2, the CO₂ product composition (stream S122) hasincreased in both the low and high nitrogen cases, due to the componentsthat leave in the crude helium product (stream S108). The CO₂ productpurity in the high nitrogen case is still below the desired 95% CO₂purity specification, so a method is required to increase the CO₂composition to meet this specification. In this case, the purity couldbe met by reducing the pressure of C101, but this would also increaserecycle power compressor further, and reduce the first enriched heliumcomposition (stream S106) and product helium composition (stream S113)as more nitrogen is rejected with the helium product. Further note thatin both cases CO₂ recovery is 100%, since CO₂ is rejected from the crudehelium product stream and returned to the process, and helium recoveryis 98%, which was the constraint applied to the optimization process.

TABLE 2 Feed composition (mol %) S106 composition (mol %) S108composition (mol %) Figure No. He H₂ N₂ C₁ Ar CO₂ He H₂ N₂ C₁ Ar CO₂ HeH₂ N₂ C₁ Ar CO₂ 1 (low N₂ 0.35 0.01 3.00 0.20 0.06 96.38 13.27 0.3562.69 1.61 0.98 21.11 42.77 1.11 54.66 0.61 0.85 0.00 feed) 1 (high N₂0.35 0.01 7.00 0.20 0.06 92.38 3.55 0.09 74.37 1.17 0.54 20.28 14.760.39 83.67 0.57 0.61 0.00 feed) 1 (N₂ PSA) 0.35 0.01 3.00 0.20 0.0696.38 11.20 0.29 66.53 1.31 1.00 19.67 97.46 2.54 0.00 0.00 0.00 0.00 2(low N₂ 0.35 0.01 3.00 0.20 0.06 96.38 31.44 0.53 47.06 1.40 0.76 18.8269.76 1.17 28.25 0.37 0.45 0.00 feed, no intermediate reboiler) 2 (lowN₂ 0.35 0.01 3.00 0.20 0.06 96.38 31.63 0.54 46.93 1.39 0.76 18.75 69.921.20 28.07 0.36 0.45 0.00 feed, intermediate reboiler) 2 (high N₂ 0.350.01 7.00 0.20 0.06 92.38 5.09 0.13 74.32 1.15 0.53 18.79 19.86 0.4978.55 0.53 0.57 0.00 feed, no intermediate reboiler) 2 (high N₂ 0.350.01 7.00 0.20 0.06 92.38 5.17 0.13 74.24 1.14 0.53 18.78 20.16 0.5078.26 0.52 0.56 0.00 feed, intermediate reboiler) 2 (low N₂ 0.35 0.013.00 0.20 0.06 96.38 29.03 0.50 49.43 1.21 0.79 19.03 98.30 1.70 0.000.00 0.00 0.00 feed, no intermediate reboiler) N₂ PSA) 3 (low N₂ 0.350.01 3.00 0.20 0.06 96.38 62.94 1.16 15.38 0.31 0.19 20.01 92.08 1.706.09 0.05 0.07 0.00 feed, no intermediate reboiler) 3 (high N₂ 0.35 0.017.00 0.20 0.06 92.38 58.67 1.05 19.95 0.30 0.13 19.90 90.00 1.61 8.280.05 0.05 0.00 feed, no intermediate reboiler) 3 (low N₂ 0.35 0.01 3.000.20 0.06 96.38 62.62 1.08 15.80 0.31 0.19 20.00 92.00 1.59 6.28 0.050.08 0.00 feed, intermediate reboiler) 4 0.35 0.01 7.00 0.20 0.06 92.3863.93 1.18 14.56 0.23 0.09 20.01 92.52 1.70 5.70 0.04 0.04 0.00 5 0.350.01 7.00 0.20 0.06 92.37 64.43 0.89 14.36 0.23 0.09 20.00 100.00 0.000.00 0.00 0.00 0.00 CO₂ Recycle recompression compression Total CO₂ HeFigure No. Power (MW) Power (MW) Power (MW) Recovery Recovery 1 (low N₂feed) 2.67 0.94 3.61 100.0% 98.0% 1 (high N₂ feed) 3.19 2.74 5.93 100.0%98.0% 1 (N₂ PSA) 2.85 1.41 4.27 100.0% 98.0% 2 (low N₂ feed, nointermediate reboiler) 2.22 0.24 2.47 100.0% 99.1% 2 (low N₂ feed,intermediate reboiler) 1.73 0.24 1.98 100.0% 99.1% 2 (high N₂ feed, nointermediate reboiler) 2.60 1.92 4.52 100.0% 99.7% 2 (high N₂ feed,intermediate reboiler) 2.57 1.88 4.44 100.0% 99.2% 2 (low N₂ feed, nointermediate reboiler, N₂ PSA) 2.16 0.41 2.57 100.0% 99.1% 3 (low N₂feed, no intermediate reboiler) 2.16 0.08 2.25 100.0% 99.9% 3 (high N₂feed, no intermediate reboiler) 2.27 0.10 2.37 100.0% 99.9% 3 (low N₂feed, intermediate reboiler) 1.98 0.08 2.07 100.0% 99.9% 4 2.88 0.082.96  99.1% 99.8% 5 3.00 0.14 3.14  99.1% 99.8%

The process exemplified in FIG. 2 improves upon the cycle of FIG. 1.Like FIG. 1, FIG. 2 and its accompanying description are included toprovide necessary background information for subsequent Figuresdepicting embodiments of the invention and to establish the state of theart. The process depicted in FIG. 2 includes a stripping column C102 inplace of the two separators C100 and C101 used in the system of FIG. 1,allowing a significant reduction in power. The reduction in power isbecause less power is required to recompress the CO₂ back to pipelinepressure, since its pressure is maintained high. Part of therefrigeration that was carried out by evaporating CO₂ in FIG. 1 is nowcarried out by integrating the heat required for the main reboiler(streams S132 and S133) into the heat exchanger HX100. Furtherefficiency improvements are achieved by adding an optional intermediatereboiler (streams S130 and S131) to the column. Since the intermediatereboiler is further up the column, it provides a colder stream that canbe integrated into heat exchanger HX100 to provide refrigeration at alower temperature than that provided by the main column reboiler. Bothlow N₂ and high N₂ feed compositions, as well as embodiments with andwithout an intermediate reboiler, were considered as exemplified in FIG.2.

In FIG. 2, the features that are the same as in FIG. 1 have been labeledwith the same reference numerals. The feed stream S100 has thecomposition shown in Table 1. An example in which the feed stream S100has a low N₂ feed composition will be considered first. The feed streamS100 is dried in TSA A101 and combined with the compressed offgas S110from the PSA A100. The combined stream S103 is then cooled in exchangerHX100 to give stream S104 at about −54° C., at which point the streamhas mostly been liquefied (the liquid fraction is around 99.5%). StreamS104 is then dropped in pressure via valve V103 to reach the operatingpressure of stripping column C102, which in this case is about 40 bar,to give stream S125, which is then fed to the top stage of strippingcolumn C102. C102 is a packed or trayed distillation column designed toallow vapor/liquid contacting, as is well known in the art. In thiscase, C102 has been modeled with 10 theoretical stages, although more orfewer could easily be used to effect the separation.

A stripping column is a type of distillation column in which there is areboiler but no overhead condenser, with the reflux liquid beingsupplied only by the liquid provided by the feed stream. In this case,stripping column C102 comprises not only a main reboiler but also anoptional intermediate reboiler. Both of these reboilers are providedwith the heat they require by integration into heat exchanger HX100. Themain (or bottom) reboiler is integrated by taking the stream leaving thebottom stage of the column, S132, and passing this to HX100 where it isheated and partially vaporized, to provide the upward flowing vapor forthe bottom part of column C102 in stream S133. In this case stream S132is at −23° C. and stream S133 is at −13° C. This provides refrigerationfor the mid-part of the cooling curve of HX100. The intermediatereboiler functions by taking a liquid stream S130 leaving, in this case,the middle of the column (i.e. leaving the 5th theoretical stage of thecolumn C102 as it is modeled within Aspen Plus) and passing this toHX100 where it is heated and partially vaporized to provide upwardflowing vapor for the top part of the column C102 in stream S131. Inthis case stream S130 is at −52° C. and stream S133 is at −26° C. Thisprovides refrigeration for the lower part of the cooling curve of HX100.

Around a third of the refrigeration required to condense the feed streamS100 is provided by the reboiler or reboilers within C102, but most ofthe refrigeration comes from reheating the helium-lean liquid CO₂ streamS115 exiting the bottom of C102. Stream S115 is split into a number ofstreams, which are warmed in HX100. The streams into which stream S115are divided provide refrigeration at different pressure, and thereforetemperature, levels as previously described with respect to FIG. 1. Thesplit between these streams and the pressure to which they are reducedor pumped is determined so as to optimize the process.

In this case some of stream S116 is dropped in pressure through valveV101 to about 6.0 bar so that it boils at a cold enough temperature toprovide a sufficient temperature difference at the cold end of heatexchanger HX100. This stream S118 after valve V101 is the coldest partof the process. The optimization has constrained the temperature of S118to be greater than the freezing point of CO₂, and is therefore at animposed lower limit of −56° C. This stream is only a small amount of thetotal flow of stream S115, about 5%, to open the heat exchanger coolingcurve at the cold end. The rest, stream S117, is maintained at thecolumn pressure of 40 bar, as the pressure required for the stream toboil at the optimal conditions was determined by the optimizer to be thesame as the column pressure. In scenarios employing a high N₂ feed,however, V102 is used to reduce the pressure of stream S117 to a lowerpressure, corresponding to a lower temperature. Part of the stream mayalso be at a third pressure (not shown) to further optimize theperformance of the heat exchanger, thereby reducing the subsequent powerfor recompression, but that was not required in this case.

Compressors K101 and K100 are used, first to recompress the recycledstream S109, second to compress the low pressure warmed CO₂ stream S120to the pressure of the higher pressure stream S121, and then finally forcompression to the product pressure (these two stages of compression areshown as one machine K100 with an intermediate feed stream in FIG. 2).

The products from the process are the CO₂ product stream S122, whichcontains substantially all of the CO₂ from feed S100, and a crude heliumproduct stream S108 that can be further purified and liquefied toproduce a pure helium stream. The performance of this stripping columncycle is summarized in Table 2.

Table 2 shows that the stripping column cycle depicted in FIG. 2 is animprovement over the double flash cycle of FIG. 1, although this comeswith the added complexity of a distillation column and reboilersintegrated into the main exchanger HX100. It is apparent that,particularly with low N₂ feed, there is a significant reduction in powerconsumption and a higher concentration of helium in streams S106 andS108, indicating a benefit that will be realized by a smaller PSA (A100)and reduction in the cost of purifying the crude helium. Note, however,that with a high N₂ feed there is a deterioration in the performance ofthe stripping column cycle, as the increased nitrogen in the feedaffects this process in much the same way that it affects the doubleflash cycle due to an increase in the nitrogen in streams S106 and S108.

The optimum pressure for column C102 as depicted in FIG. 2, with bothhigh and low N₂ feeds and both with and without an intermediatereboiler, is determined by process optimization and the results areshown in Table 3. As shown in Table 3, with low nitrogen in the feed thepressure is reduced across V103 to give an operating pressure in thecolumn C102 of just over 40 bar for the two cases shown (with andwithout an intermediate reboiler). However, with high nitrogen in thefeed the column pressure is maintained high but pressure is droppedacross V102 to achieve the optimum pressure for the higher pressure CO₂refrigeration stream. Table 3 also shows that the intermediate reboilergives a significant benefit over a single reboiler when there is lownitrogen in the feed, where there is a benefit of 0.49 MW but gives onlya 0.08 MW benefit when there is a high level of nitrogen in the feed.

TABLE 3 Low N₂ High N₂ Low N₂ High N₂ Feed, Feed, Feed, No Feed, NoIntermediate Intermediate intermediate intermediate reboiler reboilerreboiler reboiler C102 pressure (bar) 40.48 47.00 40.30 47.00Intermediate reboiler duty (MW) 5.89 0.40 0.00 0.00 Main reboiler duty(MW) 2.99 4.50 8.81 5.06 S116 flow as a fraction of S115 0.05 0.06 0.080.06 S118 pressure (bar) 6.00 6.85 6.22 6.37 S119 pressure (bar) 40.4835.88 40.30 35.75 K101 power (MW) 0.24 1.88 0.24 1.92 K100 power (MW)1.73 2.57 2.22 2.60 CO₂ recovery (%) 100.0 100.0 100.0 100.0 He recovery(%) 99.1 99.2 99.1 99.7 S108 helium purity (mol %) 69.92 20.16 69.7619.86

The examples of FIG. 2, as reported in Table 3, show that a cycle isrequired that can handle the Low and High N₂ Feed streams equally well.The double flash and the stripping columns of FIGS. 1 and 2 do well withthe Low N₂ Feed composition, but their performance, as measured in powerconsumption and the helium composition of the helium product streamS108, needs to be improved. Also, with the High N₂ Feed, there is a needto enrich the CO₂ product composition to meet a pipeline requirementof >95% CO₂. These issues are addressed in the following inventiveembodiments of FIGS. 3 through 7.

FIG. 3 shows a process that incorporates a CO₂ wash in the mainseparation column. This embodiment differs from the stripping columncycle of FIG. 2 in that the distillation column C103 has a section abovethe main feed where the overhead vapor is washed with a streamcomprising liquid CO₂ in order to further reduce the amount of nitrogenin the first helium-enriched stream S106.

In FIG. 3, the features that are the same as in FIG. 1 or FIG. 2 havebeen labeled with the same reference numerals. The feed stream S100 hasthe composition shown in Table 1. An embodiment in which the feed streamS100 has a low N₂ feed composition will be considered first. The feedstream is dried in TSA A101 and combined with the compressed offgas fromthe PSA A100 in stream S110. The combined stream S103 is cooled in heatexchanger HX100 to give stream S104 at −17° C., at which point thestream has mostly been liquefied (the liquid fraction is around 99.1%).Stream S104 is then dropped in pressure via valve V103 to reach theoperating pressure of the column C103, which in this case is 41 bar, togive stream S125. Stream S125 is then fed to the stage within columnC103 determined to be the optimum location; in this case the streamenters onto the 6th theoretical stage from the top of the column C103.C103 is a packed or trayed distillation column designed to allowvapor/liquid contacting, as is well known in the art. In this case,column C103 has been modeled with 15 theoretical stages, although moreor fewer could easily be used to effect this separation.

As with the stripping column in FIG. 2, the distillation column C103 hasbeen modeled with and without an intermediate reboiler. Shown in FIG. 3is the case without an intermediate reboiler. The main reboiler is asdiscussed in the description of the stripping column embodied in FIG. 2,however in FIG. 3 more detail has been given regarding the flowarrangement in the main reboiler. The liquid stream taken from thebottom stage of C103, stream S132, is at −18° C. and is heated andpartially vaporized in HX100 to −8° C. The two-phase stream from HX100,stream S133, is separated in phase separator C104 into a liquidfraction, stream S115, and a vapor fraction, stream S134, that isreturned to column C103 to provide the upward-flowing vapor streamrequired by the distillation process.

Some of the refrigeration required to condense the feed stream isprovided by the reboiler or reboilers within C103, but most of therefrigeration comes from reheating the helium-lean liquid stream S115exiting phase separator C104. Stream S115 is split into a number ofstreams that are warmed in HX100. The streams into which stream S115 aredivided provide refrigeration at different pressure, and thereforetemperature, levels. The split between these streams and the pressure towhich they are reduced or pumped is determined so as to optimize theprocess.

In this case some of this liquid, in stream S116, is dropped in pressurethrough valve V101 to 7.3 bar so that it boils at a cold enoughtemperature to provide sufficient temperature difference at the cold endof the heat exchanger. The resulting stream S118 exiting valve V101 isthe coldest part of the process, and the optimization has constrainedthis temperature to be greater than the freezing point of CO₂. Thisstream S116 is only a small amount of the total flow of stream S115,about 6.6%, to open the heat exchanger cooling curve at the cold end.The rest, in stream S117, is maintained at the column pressure of 41bar. Part of stream S115 may also be at a third pressure (not shown) tofurther optimize the performance of the heat exchanger HX100, therebyreducing the subsequent power for recompression, but this was notrequired in this case.

The difference between the inventive embodiment depicted in FIG. 3 andthe background example of FIG. 2 is that in FIG. 3 stream S117 iswithdrawn from the exchanger HX100 mid-way through warming, enteringHX100 at −7.9° C. and leaving at 4.4° C. The temperature at which thestream is withdrawn from HX100 is determined by the requirement for aliquid CO₂ stream to wash nitrogen from the overhead vapor in columnC103. The lower this temperature, the more liquid is available forwashing in C103. Stream S140, withdrawn from HX100 at 4.4° C., isseparated into a liquid fraction (stream S142) and a vapor fraction(S141) by phase separation in vessel C105. Although separator C105 isreferred to herein as a phase or flash separator, a distillation columnhaving multiple stages may be used as well. Stream S141 is returned toHX100 and is warmed to give stream S121, which is part of the productCO₂ stream S122. Liquid stream S142 is returned to HX100 to be cooled to−49° C. before being pumped via P101 (to overcome pressure losses andstatic head) and fed to the top of column C103, where it is used to washnitrogen from the overhead vapor stream in column C103. In this manner,the nitrogen composition of the first helium-enriched stream S106 isreduced to levels below those achievable in a stripping column like thatdepicted in FIG. 2.

Compressors K101 and K100 are used in the embodiment shown in FIG. 3,first to recompress the recycled stream S109 exiting the PSA A100,second to compress the low pressure warmed CO₂ stream S120 to thepressure of the higher pressure stream S121, and then finally forcompression to the product pressure (these two stages of compression areshown as one machine K100 with an intermediate feed stream in FIG. 3).

The products from the process of FIG. 3 are the CO₂ product stream S122,which contains substantially all of the CO₂ from feed S100, and a crudehelium product stream S108 that can be further purified and liquefied toproduce a pure helium stream. The performance of the wash column cycleof FIG. 3 is summarized in Table 2.

Table 2 shows that the wash column cycle of FIG. 3 with the Low N₂ Feedis comparable in power consumption with the stripping column cycle ofFIG. 2, but it results in helium compositions in streams S106 and S108around double those of FIG. 2, indicating the potential benefits to thedownstream purification and liquefaction process. However, it is at theHigh N₂ Feed conditions where the benefits are more noticeable, with thewash column cycle of FIG. 3 showing only a slight power increase atthese conditions without the noticeable reduction in performance seen inthe High N₂ Feed examples of FIG. 2. Table 2 also shows that anintermediate reboiler can be used with the wash column of FIG. 3(similar to the intermediate reboiler depicted in FIG. 2), resulting inabout a 10% reduction in power consumption but adding the extracomplexity involved in incorporating an intermediate reboiler.

Additional embodiments of the systems and methods of the presentinvention incorporate rejection of nitrogen from the helium-depleted CO₂product stream, particularly in the case of scenarios in which the feedis similar to the High N₂ Feed, in order to reach a given CO₂specification (in this case 95% CO₂ in the product stream S122). Anembodiment of the process incorporating nitrogen rejection is shown inFIG. 4. FIG. 4 differs from the wash column cycle of FIG. 3 by theseparators C106 and C107 used to flash more volatile components,particularly nitrogen, from the product CO₂. The washing process in FIG.3 has the effect of reducing nitrogen in the first helium-enrichedstream S106, which forces the nitrogen into the bottom stream S115. Theprocess of FIG. 4 allows that nitrogen to be separated from the CO₂.

In FIG. 4, the features that are the same as in FIGS. 1 through 3 havebeen labeled with the same reference numerals. The feed stream S100 hasthe composition shown in Table 1. In the embodiment depicted in FIG. 4,only the high N₂ feed composition is considered, as it is this feedcomposition that requires increasing the CO₂ product purity to aconcentration above that in the feed stream. The feed stream S100 isdried in TSA A101 and combined with the compressed offgas from PSA A100in stream S110. Combined stream S103 is then cooled in heat exchangerHX100 to give stream S104 at −46° C., at which point the stream hasmostly been liquefied (the liquid fraction is around 97.3%). Stream S104is then dropped in pressure via valve V103 to reach the operatingpressure of the column C103, which in this case is 39 bar, to givestream S125. S125 is then fed to a stage within C103 determined to bethe optimum location; in this case stream S125 enters onto the 6ththeoretical stage from the top of the column C103. C103 is a packed ortrayed distillation column designed to allow vapor/liquid contacting, asis well known in the art. In this case, C103 has been modeled with 15theoretical stages, although more or fewer could easily be used toeffect this separation.

Since the exemplary process depicted in FIG. 4 is focused on the High N₂Feed composition (although the process of FIG. 4 could be employed witha low N₂ feed, a high N₂ feed, or a feed having an intermediate N₂composition), and as discussed above the intermediate reboiler does nothave a great impact with the High N₂ Feed stream, the wash columnprocess in FIG. 4 has been modeled with nitrogen rejection and only onemain reboiler. The main reboiler is as discussed in the description ofFIG. 3. The liquid stream from the bottom stage of C103, stream S132, isat −46.4° C. and is heated and partially vaporized in HX100 to −27.5° C.The two-phase stream from HX100, stream S133, is separated in C104 intoa liquid fraction, stream S115, and a vapor fraction stream S134 that isreturned to column C103 to provide the upwards-flowing vapor streamrequired by the distillation process.

Some of the refrigeration required to condense the feed stream S100 isprovided by the reboiler for column C103, but most of the refrigerationcomes from reheating the helium-lean liquid stream S115 exiting phaseseparator C104. Stream S115 is split into a number of streams that arewarmed in HX100. The streams into which stream S115 are divided providerefrigeration at different pressure, and therefore temperature, levels.The split between these streams and the pressure to which they arereduced or pumped is determined so as to optimize the process.

In this case some of this liquid, in stream S116, is dropped in pressurethrough valve V101 to 8.1 bar so that it boils at a cold enoughtemperature to provide sufficient temperature difference at the cold endof the heat exchanger HX100. This stream S118 after valve V101 is thecoldest part of the process, and the optimization has constrained thistemperature to be greater than the freezing point of CO₂. This stream isonly a small amount of the total flow of stream S115, about 3.6%, due tothe fact that some of the higher pressure CO₂ is recycled to this pointonce nitrogen has been stripped from stream 3117, thereby making up thedifference to produce the refrigeration at the cold end of the process.The rest of stream S115, in stream S117, is maintained at the columnpressure of 39 bar.

The difference between the embodiments depicted in FIG. 4 and FIG. 3 isthat stream S117 is warmed in heat exchanger HX100 to only −13° C. inthe system of FIG. 4. Stream S150, withdrawn from HX100 at −13° C., isseparated into a liquid fraction (stream S151) and a vapor fraction(stream S152) fraction by phase separation in separator C106. Althoughseparator C106 is referred to herein as a phase or flash separator, adistillation column having multiple stages may be used as well. Thepurpose of this section of the process is to reject nitrogen from theCO₂ product stream. Stream S150 comprises about 4.1% nitrogen, whereasthe vapor stream leaving separator C106 comprises about 29.2% nitrogen,or a little more than a third of the nitrogen that was in stream S150prior to separation in C106.

Stream 3151 is then returned to HX100, where it is warmed and withdrawnas stream S140 at 1.1° C. and is separated into a liquid fraction(stream S142) and a vapor fraction (stream S141) in vessel C105. StreamS141 is returned to HX100 and is warmed to give stream 3121, part of theproduct CO₂ stream S122. Liquid stream S142 is returned to HX100 to becooled to −46° C. before being pumped via pump P101 (to overcomepressure losses and static head) and fed to the top of column C103,where it is used to wash nitrogen from the overhead vapor stream, thusreducing the nitrogen composition of the first helium-enriched streamS106 to levels below that achievable in the stripping column of FIG. 2.

The nitrogen-enriched vapor stream S152 from separator C106 is thenreturned to HX100 to be re-cooled to condense CO₂ from the stream,increase the concentration of nitrogen in the vent stream, and minimizelosses of CO₂ in the nitrogen vent. This cooled stream S153 leaves HX100at −49° C., wherein 65% of stream S153 is in the liquid phase. Inseparator C107, stream S153 is separated into a nitrogen-enriched vaporstream S154 and a liquid stream S155. The nitrogen enriched stream S154comprises 73.0% nitrogen and 25.0% CO₂. The 25.0% CO₂ composition instream S154 is a limit placed upon the process and imposed by the use ofa constraint within the process optimizer. This value, which representsa loss of CO₂ from the process of less than 1%, can be altered bychanging temperatures and pressures within the process. Alternatively,some or all of the CO₂ in this vent stream S154 could be recovered usingwell-known adsorption, absorption or membrane systems to return theprocess to close to 100% CO₂ recovery.

The nitrogen-enriched stream S154 is then warmed within HX100 and ventedfrom the process as stream S157. The liquid stream S155 from separatorC107 is reduced in pressure via valve V104 to the pressure of streamS118 and combined to make up the rest of the low pressure CO₂ requiredfor the cold end refrigeration duty, as mentioned previously.

Compressors K101 and K100 are used, first to recompress the recycledstream S109, second to compress the low pressure warmed CO₂ stream S120to the pressure of the higher pressure stream S121, and then finally forcompression to the product pressure (these two stages of compression areshown as one machine K100 with an intermediate feed stream in FIG. 4).

The products from the process depicted in FIG. 4 are: (1) the CO₂-richproduct stream S122, with the CO₂ composition increased to 95% from thefeed composition of 92.38% (Stream S122 contains nearly all of the CO₂from feed S100, less the small amount lost with the nitrogen vent streamS157); (2) a crude helium product stream S108 that can be furtherpurified and liquefied to produce a pure helium stream; and (3) anitrogen-rich vent stream S157. When nitrogen rejection is employed, theresulting nitrogen vent stream S157 may contain some residual CO₂. ThisCO₂ can be easily recovered using a variety of well known processes suchas absorption, adsorption, or membrane separation systems.

The performance of the process of FIG. 4, incorporating a CO₂ wash andnitrogen rejection, is summarized in Table 2. As shown in Table 2, thepower consumption has increased with the addition of the nitrogenrejection, from 2.37 MW to 2.96 MW; CO₂ recovery has reduced from 100%to 99.1% due to the loss of CO₂ in the nitrogen vent, and the productCO₂ composition has been increased to meet the required value of 95.0%from the previous value of 92.74%.

Examining the results in Table 2, one can see that the wash columncycle, with or without nitrogen rejection, reaches a helium purity instream S108, after CO₂ recovery from the first helium-enriched streamS106/S107, of greater than 90%. In the scenario embodied in FIG. 4, withnitrogen rejection, stream S108 comprises 92.52% helium, 5.7% nitrogen,and 1.7% hydrogen (hydrogen is a light component and around two thirdsof the hydrogen in the feed stream S100 ends up in this stream), plus394 ppm methane and 361 ppm argon.

It was found that it is possible to design the PSA system A100 to removesubstantially all of the nitrogen and argon as well as CO₂ from theproduct helium stream S108. However, to remove hydrogen, a catalyticcombustor R100 is required, as shown in the embodiment depicted in FIG.5. The catalytic combustor R100 may be a unit employing a palladium- orplatinum-containing catalyst, or any other catalyst suitable for thecombustion of hydrogen and trace hydrocarbons. The combustion needs asource of oxygen, which can be air, oxygen enriched air, or oxygen. Inthis case, air was added and controlled in the optimization so thatthere was a small excess of oxygen over that required by combustion. Asa result, the amount of air added was controlled to give 100 ppm oxygenin the converted stream S160 exiting the combustor R100. The hydrogen-and methane-free stream S160 is then purified in PSA A100 to give a purehelium stream S161 and an offgas stream S109. Unlike in the previousexamples, stream S109 contains minor amounts of oxygen, which typicallyis not detrimental as it is a minor component, and water as a product ofthe oxidation reactions that take place in R100. It therefore makessense that the recycle stream S110 from the PSA A100 should be recoveredto a point upstream of the water removal TSA A101 so as not to introducewater into the low temperature process, which could freeze or form solidCO₂ hydrates and create a blockage in heat exchanger HX100, although therecycle stream could also be dried separately.

Table 2 shows the results of the process embodied in FIG. 5, wherehelium product stream S161 now comprises 100% helium and there is norequirement for further purification before the helium can be liquefied.The products from the process in FIG. 5 are therefore: (1) the CO₂-richproduct stream S122, with a CO₂ composition increased to 95% from thefeed composition of 92.38% (Stream S122 contains nearly all of the CO₂from feed stream S100, less the small amount lost with the nitrogen ventstream S157); (2) a pure helium product stream S161, which can beliquefied without further purification to produce the product purehelium stream; and (3) a nitrogen-rich vent stream S157.

Note that a nitrogen vent stream is not required in order to obtain apure helium product. For example, a pure helium product can be producedfrom the process described in FIG. 3 (with modifications as describedabove such as a catalytic combustor and related improvements to the PSA)for situations in which nitrogen rejection is not necessary, forinstance with low nitrogen in the feed stream or a lower product CO₂purity requirement.

Further, the PSA design depicted in FIG. 5 as described above may beincorporated into other configurations of the process, and suchconfigurations are considered within the scope of the present invention.For example, a catalytic combustor and PSA may be employed to improvethe double flash cycle depicted in FIG. 1 or the stripping columnconfiguration depicted in FIG. 2.

Also note that, in embodiments of the invention that incorporate a CO₂wash in the distillation column, it is possible to omit the PSA entirelyand still achieve a desired level of helium purity. For example, twosuch possible configurations are shown in FIGS. 6 and 7, whichincorporate a recycle CO₂ wash and a feed CO₂ wash (respectively). InFIGS. 6 and 7, the features that are the same as in FIGS. 1 through 5have been labeled with the same reference numerals. The process depictedin FIG. 6 is the same as that shown in FIG. 3 and previously described,except that helium-enriched stream S107 is not separated or purifieddownstream after exiting heat exchanger HX100 and is instead recovereddirectly as a product.

Similarly, in the process depicted in FIG. 7, helium-enriched streamS107 is recovered directly as a product. In FIG. 7, however, the CO₂wash stream fed to column C103 is derived from the feed stream S100rather than from a recycle stream. As shown in FIG. 7, the dried feedstream S102 is partially cooled in heat exchanger HX100. This partiallycooled stream S161 is then separated into a liquid fraction (streamS162) and a vapor fraction (S161) by phase separation in vessel C105.Although separator C105 is referred to herein as a phase or flashseparator, a distillation column having multiple stages may be used aswell. Stream S161 is returned to HX100 and is further cooled to atemperature at which the stream has been mostly liquefied to give streamS104. Liquid stream S162 is also returned to HX100 to be further cooled,forming CO₂ wash stream S163. Stream S163 is fed to the top of columnC103, where it is used to wash nitrogen from the overhead vapor streamin column C103.

Another embodiment, which includes a membrane unit M100, is shown inFIG. 8. Embodiments of the invention with a membrane unit M100 areparticularly well-suited for feed streams containing higherconcentrations of nitrogen and/or methane.

In FIG. 8, the features that are the same as in FIGS. 1 to 7 have beenlabeled with the same reference numerals

The addition of a membrane unit M100 may be desirable for retrofitcases, providing an option requiring only simple system modifications tomeet desired CO₂ purity requirements and that do not significantlyincrease power requirements.

While many membrane systems require ancillary equipment such ascompressors, embodiments of the present invention using the membraneunit may use an existing compressor, thereby providing synergy with thesystems described above.

With reference to FIG. 8, the present invention then also relates to amethod for recovering helium from a feed stream S100 containing helium,carbon dioxide and at least one of methane and nitrogen using a membraneseparator M100. The feed stream may have a CO₂ concentration of at least50 mole % CO₂. The method comprises introducing separator feed streamS125 into separator C110. The separator feed stream S125 comprises atleast a portion of feed stream S100. Separator feed stream S125 isseparated into a first helium-enriched stream S106 and a firstCO₂-enriched stream S115. The first helium-enriched stream S106 and thefirst CO₂-enriched stream S115 are withdrawn from separator C110.

The separator C110 may be a pressure swing adsorption separator.Pressure swing adsorption separators for separating He and CO₂ are knownin the art.

The separator C110 may be a fractionator. As used herein, a“fractionator” includes such devices as distillation columns, flashdrums, rectification columns, stripping columns and the like.

In case the separator C110 is a fractionator, and the fractionator is adistillation (stripping) column, the first helium-enriched stream S106may be withdrawn from an upper location of the distillation column, andthe first CO₂-enriched stream (8115) may be withdrawn from a lowerlocation of the distillation column. The method may further comprisecooling the feed stream S100 (e.g. in heat exchanger HX100) to form theseparator feed stream S125. The method may further comprise feeding aliquid stream comprising CO₂ to an upper portion of the distillationcolumn as a CO₂ wash stream S163. Separator feed stream S125 may beintroduced into the distillation column at an location intermediate theupper location of the distillation column and the lower location of thedistillation column (i.e. between the introduction location of the CO₂was stream S163 and the withdrawal location of the first CO₂-enrichedstream S115).

While shown with the distillation column in FIG. 8, any of theconfigurations of the heat exchanger HX100 and various separators (C100,C101, C102, C103, C104, C105, C106, C107) described above may be usedwith the membrane unit M100.

The first helium-enriched stream S106 may comprise one or morecombustible components. When the first helium-enriched stream S106contains an undesirable amount of combustible components, the method mayfurther comprise catalytically combusting the combustible components inthe first helium-enriched stream in the presence of oxygen to at leastpartially convert the combustible components to CO₂ and H₂O therebyforming a combustible component-depleted helium-enriched stream. Thepressure swing adsorption unit feed stream S107 may then comprise thecombustible component-depleted helium-enriched stream as the at least aportion of the first helium-enriched stream S106. The combustiblecomponents may be combusted in a catalytic combustor as described abovefor FIG. 5. The discussion of the catalytically combusting thecombustible components for FIG. 5 may be applied to the processdescribed in FIG. 8.

The method comprises introducing a pressure swing adsorption unit feedstream S107 into a pressure swing adsorption unit A100. The pressureswing adsorption unit feed stream S107 comprises at least a portion ofthe first helium-enriched stream S106. Pressure swing adsorption unitfeed stream S107 is separated into a helium-rich product stream S108 anda helium-lean stream (S109). The helium-rich product stream S108 and thehelium-lean stream (S109) are withdrawn from the pressure swingadsorption unit A100.

The method comprises compressing a compressor feed stream S205 in acompressor K101 to form a compressor effluent stream S110. Thecompressor feed stream S205 comprises the helium-lean stream (S109) anda helium-enriched permeate stream S203.

The method comprises introducing a first portion S201 of the compressoreffluent stream S110 into a membrane separation unit M100. The firstportion S201 of the compressor effluent stream S110 is separated in themembrane separation unit M100 to form the helium-enriched permeatestream S203 and a helium-depleted non-permeate stream S204. Thehelium-enriched permeate stream S203 and the helium-depletednon-permeate stream S204 are withdrawn from the membrane separation unitM100. The helium-enriched permeate stream S203 is recycled to thecompressor K101. The helium-depleted non-permeate stream S204, which isenriched in N₂ and CH₄ and still at high pressure, may be mixed with theproduct CO₂ stream, vented, or burned for power.

The method comprises introducing a second portion S202 of the compressoreffluent stream S110 into the separator C110. The second portion S202 ofthe compressor effluent stream S110 may be introduced into separatorC110 separately from the separator feed stream S125. The second portionS202 of the compressor effluent stream S110 may be blended with the atleast a portion of the feed stream S100 and the mixture introducedtogether as the separator feed stream S125.

The first portion S201 and the second portion S202 may be dividedportions of the compressor effluent stream S110. The ratio of the molarflow rate of the first portion S201 of the compressor effluent streamS110 to the molar flow rate of the second portion S202 of the compressoreffluent stream S110 may be varied to effect the recovery and purity ofeach of the resulting He and CO₂ product streams. The ratio of the molarflow rate of the first portion S201 of the compressor effluent streamS110 to the molar flow rate of the second portion S202 of the compressoreffluent stream S110 may range from 0.25 to 0.90 or may range from 0.60to 0.85.

The present invention also relates to a system for recovering heliumfrom a feed stream S100 containing helium, carbon dioxide and at leastone of methane and nitrogen. The feed stream S100 may have a CO₂concentration of at least 50 mole % CO₂.

With reference to FIG. 8, the system comprises a separator C110operatively disposed to receive a separator feed stream S125. Theseparator feed stream S125 comprises at least a portion of the feedstream S100. The separator C110 is operatively configured to separatethe separator feed stream S125 into a first helium-enriched stream S106and a first CO₂-enriched stream S115.

As discussed above, the separator C110 may be a pressure swingadsorption separator. The separator C110 may be a fractionator.

When the separator C110 is a fractionator, and the fractionator is adistillation (stripping) column, the distillation column has a firstoutlet operatively disposed to withdraw the first helium-enriched streamS106 where the first outlet is located in an upper portion of thedistillation column as shown in FIG. 8. The distillation column has asecond outlet operatively disposed to withdraw the first CO₂-enrichedstream S115 where the second outlet is located in a lower portion of thedistillation column. The distillation column has a first inletoperatively disposed to introduce the separator feed stream S125. Thefirst inlet is located at a position intermediate the upper portion ofthe distillation column and the lower portion of the distillationcolumn. The distillation column has a second inlet operatively disposedto introduce a CO₂ wash stream. The second inlet is located in the upperportion of the distillation column as shown in FIG. 8.

The system may further comprise one or more heat exchangers HX100operatively configured to cool the at least a portion of the feed streamS100 to form the separator feed stream S125 by indirect heat transferwith a portion or all of the first helium-enriched stream S106 and aportion or all of the first CO₂-enriched stream S115 thereby heating theportion or all of the first helium-enriched stream S106 and the portionor all of the first CO₂-enriched stream S115.

As discussed for the method, the first helium-enriched stream maycomprise one or more combustible components. In case the firsthelium-enriched stream comprises one or more combustible components, thesystem may further compris a catalytic combustor (not shown) containinga catalyst, which is operatively configured to combust the one or morecombustible components in the first helium-enriched stream. the one ormore combustible components may be reacted in the presence of oxygen toat least partially convert the combustible components to CO₂ and H₂Othereby forming a combustible component-depleted helium-enriched stream.The pressure swing adsorption unit feed stream S107 then comprises thecombustible component-depleted helium-enriched stream as the at least aportion of the first helium-enriched stream S106.

The system comprises a pressure swing adsorption unit A100. The pressureswing adsorption unit A100 is operatively configured to separate apressure swing adsorption unit feed stream S107 into a helium-richproduct stream S108 and a helium-lean stream S109. The pressure swingadsorption unit feed stream S107 comprises at least a portion of thefirst helium-enriched stream S106.

The system comprises a compressor K101 operatively disposed to receive acompressor feed stream S205 comprising the helium-lean stream S109 and ahelium-enriched permeate stream S203. The compressor is operativelyconfigured to compress the compressor feed stream S205 to form acompressor effluent stream S110. The compressor effluent stream S110 isdivided to form a first portion S201 and a second portion S202.

The system comprises a membrane separation unit M100 operativelydisposed to receive the first portion S201 of the compressor effluentstream S110 and operatively configured to separate the first portionS201 of the compressor effluent stream S110 into the helium-enrichedpermeate stream S203 and a helium-depleted non-permeate stream S204.

The separator C110 is operatively disposed to receive the second portionS202 of the compressor effluent stream S110.

The membrane separation unit M100 may comprise a separation module. Theseparation module may be a hollow fiber moduel or a spiral wound module.Spiral wound modules are described, for example, in Schwinge et al.,“Spiral wound modules and spacers Review and analysis,” Journal ofMembrane Science, vol. 242, pp. 129-153, ScienceDirect, 2004.

The separation module may comprise a membrane, where the membranecomprises a support. The support may comprises a material selected fromthe group consisting of polysulfone, cellulose acetate, an aromaticpolyimide, an aromatic polyamide, an aromatic polycarbonate,poly(dimethyl phenylene oxide), poly(dimethyl siloxane), and carbon.

The separation membrane may be a mixed matrix membrane. Mixed matrixmembranes are described, for example, in Aroon et al., “Performancestudies of mixed matrix membranes for gas separation: A review,”Separation and Purification Technology, vol. 75, pp. 229-242, 2010.

The separation membrane may be a facilitated transport membrane.Facilitated transport membranes are described, for example, in Ravanchiet al., “Application of membrane separation processes in petrochemicalindustry: a review,” Desalination, vol. 235, pp. 199-244, ScienceDirect,2009.

To show the impact of the membrane separation unit, the process depictedin FIG. 8 with a membrane separation unit and the process depicted inFIG. 9 without a membrane separation unit were simulated using ASPENplus version 8.6, which is commercially available software. The processdepicted in FIG. 8 was simulated using a stripping column pressure of 42bar and 57 bar. FIG. 9 was simulated using a stripping column pressureof 57 bar.

For the FIG. 8 process, the feed stream S100 has the composition shownin Table 4. When the operating pressure of stripping column C110 isgreater than the feed pressure, for example the 57 bar case, feed streamS100 is compressed in compressor K99. The feed stream S100 is dried intemperature swing adsorber (TSA) A101 and combined with the a portionS202 of compressor effluent S110 formed from the helium-lean stream S109from the pressure swing adsorption unit A100. The combined stream S103is then cooled in exchanger HX100 to give stream S104 at about −45° C.,at which point the stream has mostly been liquefied (the liquid fractionis around 99.5%) If the operating pressure of stripping column C110 isless than the feed stream pressure, for example the 42 bar case, streamS104 is expanded in pressure via valve V103 to reach the operatingpressure of stripping column C110 to give stream S125, which is then fedto the top stage of stripping column C110. C110 is a packed or trayeddistillation column designed to allow vapor/liquid contacting, as iswell known in the art. In this case, C110 has been modeled with 15theoretical stages, although more or fewer could easily be used toeffect the separation.

A stripping column is a type of distillation column in which there is areboiler but no overhead condenser, with the reflux liquid beingsupplied only by the liquid provided by the feed stream. In this case,stripping column C110 comprises not only a main reboiler but also anoptional intermediate reboiler. Both of these reboilers are providedwith the heat they require by integration into heat exchanger HX100. Themain (or bottom) reboiler is integrated by taking the stream leaving thebottom stage of the column, S132, and passing this to HX100 where it isheated and partially vaporized, to provide the upward flowing vapor forthe bottom part of column C102 in stream S133. In this case stream S132is at −42° C. and stream S133 is at −13° C. This provides refrigerationfor the mid-part of the cooling curve of HX100.

Around a quarter of the refrigeration required to cool and/or condensethe streams S100, S104 and S162 is provided by the reboiler or reboilerswithin C110, but most of the refrigeration comes from reheating thehelium-lean liquid CO₂ stream S115 exiting the bottom of C110. StreamS115 is split into a number of streams, which are warmed in HX100. Thestreams into which stream S115 are divided provide refrigeration atdifferent pressure, and therefore temperature, levels as previouslydescribed with respect to FIG. 1. The split between these streams andthe pressure to which they are reduced or pumped is determined so as tooptimize the process.

In this case some of stream S116 is dropped in pressure through valveV101 to about 9.0 bar so that it boils at a cold enough temperature toprovide a sufficient temperature difference at the cold end of heatexchanger HX100. This stream S118 after valve V101 is the coldest partof the process. The optimization has constrained the temperature of S118to be greater than the freezing point of CO₂, and is therefore at animposed lower limit of −56° C. This stream is only a small amount of thetotal flow of stream S115, about 5%, to open the heat exchanger coolingcurve at the cold end. The rest, stream S117, is dropped to the CO₂product pressure of 48.6 bar, to further optimized the performance ofthe heat exchanger, thereby reducing the subsequent power forrecompression. Part of the stream may also be at a third pressure (notshown), but that was not required in this case.

Compressor K99 is used for compressing the 48.6 bar feed to 57 bar inthe high-pressure column cases. K101 is used to recompress thecompressor feed stream S205 comprising helium-lean stream S109 from thepressure swing adsorption unit A100 and the helium-enriched permeatstream S203 from the membrane unit M100. K100 is used to compress thelow pressure warmed CO₂ stream S120 to the pressure of the higherpressure stream S121, and then finally for compression to the productpressure (these two stages of compression are shown as one machine K100with an intermediate feed stream in FIG. 8).

80% of the compressor effluent S110 forms the first portion S201 of thecompressor effluent S110 and 20% of the compressore effluent S110 formsthe second portion S202 of the compressor effluent. The first portionS201 of the compressor effluent S110 is passed to the membraneseparation unit M100 where the first portion S201 is separated to formthe helium-enriched permeate stream S203 and the helium-depletednon-permeate stream S204. The helium-enriched permeate stream S203 isrecycled back to the inlet of the compressor K101.

The products from the process are the CO₂ product stream S122, whichcontains substantially all of the CO₂ from feed S100, and a crude heliumproduct stream S108 that can be further purified and liquefied toproduce a pure helium stream.

Compositions of various streams calculated by the simulation are shownin Table 4 for the process flow diagram in FIG. 8 with the strippingcolumn at 57 bar.

The performance of this system is summarized in Table 5.

For comparison, the process depicted in FIG. 9 without a membraneseparation unit was simulated using ASPEN plus. A summary of thecompositions of various stream is shown in Table 6. The performance ofthe system shown in FIG. 9 is summarized in Table 5.

The total power requirement for FIG. 8 with the membrane separation unitis slightly lower than the total power requirement for FIG. 9 withoutthe membrane separation unit (2.94 MW vs. 3.22 MW). The He concentrationin the He product stream is greater for the case with the membraneseparation unit as compared to the He concentration for the case withoutthe membrane separation unit (98.39 vs. 97.82). The CO₂ concentration inthe CO₂ product stream is greater for the case with the membraneseparation unit as compared to the CO₂ concentration for the casewithout the membrane separation unit (93.54 vs. 92.71). The He recoveryand CO₂ recovery are slightly higher for the case without the membraneseparation unit as compared to the case with the membrane separationunit.

The process according to FIG. 8 with a membrane separation unit was alsosimulated for a stripping column at a lower pressure of 42 bar. As withthe 57 bar case, 80% of the compressor effluent S110 forms the firstportion S201 of the compressor effluent S110 and 20% of the compressoreeffluent S110 forms the second portion S202 of the compressor effluent.Resulting compositions for the process flow diagram shown in FIG. 8 withthe stripping column at a pressure of 42 bar are summarized in Table 7.The performance of the system is summarized in Table 5.

TABLE 4 Stream He H₂ N₂ CH₄ Ar CO₂ Feed S100 (mol %) 0.35 0.01 7.00 0.200.06 92.38 Overhead S106 24.23 0.40 55.29 0.45 0.33 19.29 (mol %) Heproduct S108 98.39 1.61 0.00 0.00 0.00 0.00 (mol %) CO₂ product S1220.00 0.00 6.20 0.20 0.06 93.54 (mol %) Membrane feed S201 23.98 0.0040.16 0.00 0.27 35.59 (mol %) Recycled permeate 42.27 0.00 7.38 0.000.11 50.24 S203 (mol %) Rejected non-permeate 0.13 0.18 82.17 0.69 0.4816.35 S204 (mol %)

TABLE 5 Stream FIG. 8-57 bar FIG. 8-42 bar FIG. 9-57 bar Feedcompression 0.92 n/a 0.91 power (MW) CO₂ recompression 1.06 2.25 1.40power (MW) Recycle compression 0.96 1.73 0.91 power (MW) Total power(MW) 2.94 3.98 3.22 CO₂ recovery (%) 99.8 99.6 100 He recovery (%) 99.599.3 99.7 Main reboiler duty 7.25 5.53 7.44 (MW) S116 flow as fraction0.08 0.05 0.08 of S115 flow S118 pressure (bar) 9.02 5.23 6.1 S119pressure (bar) 48.61 37.83 48.61

TABLE 6 Stream He H₂ N₂ CH₄ Ar CO₂ Feed S100 0.35 0.01 7.00 0.20 0.0692.38 (mol %) Overhead S106 15.84 0.35 67.69 0.62 0.41 15.08 (mol %) Heproduct S108 97.82 2.18 0.00 0.00 0.00 0.00 (mol %) CO₂ product 0.000.00 7.02 0.20 0.06 92.71 S122 (mol %)

TABLE 7 Stream He H₂ N₂ CH₄ Ar CO₂ Feed S100 0.35 0.01 700 0.20 0.0692.38 (mol %) Overhead S106 11.68 0.21 71.15 0.62 0.50 15.84 (mol %) Heproduct S108 98.20 1.80 0.00 0.00 0.00 0.00 (mol %) CO₂ product 0.000.00 4.77 0.18 0.05 95.00 S122 (mol %) Membrane feed 13.11 0.00 57.440.00 0.43 29.01 S201 (mol %) Recycled 33.82 0.00 11.03 0.00 0.19 54.97permeate S203 (mol %) Rejected non- 0.08 0.08 85.92 0.77 0.59 12.57permeate S204 (mol %)

At 42 bar, the CO₂ concentration in the CO₂ product stream is increasedto 95 mole % with a penalty in total power required. At this lowerpressure the column C110 would expected to operate more effectivelybecause it is further away from the critical pressure. However, at 42bar it is not possible to operate the process in FIG. 9 because the CO₂cannot dissolve that much N2 and it accumulates in the loop from S106 toA100 to S109 to C110 and back again to S106.

Benefits of the systems and methods described herein include, but arenot limited to, one or more of the following: (1) removal of both CO₂and N₂ from the overhead helium-enriched stream exiting the stripping(or distillation) column, thereby increasing the helium composition andreducing the nitrogen composition of that stream while reducing theamount of nitrogen recycled form the PSA; (2) the option to use one ormore separators in place of a distillation column; (3) the use of anoptional intermediate reboiler in the distillation column to improveoverall efficiency, especially when the N2 concentration in the feed islow; (4) recycle of liquid CO₂ to the top of the column as an optionalCO₂ wash, which strips N2 from the overhead stream and reduces N2 in thehelium-rich overhead stream, instead moving it to the CO₂ productstream; (5) removal of methane and other higher hydrocarbons via anoptional CO₂ wash, further eliminating impurities from the overheadenriched helium stream that would otherwise require removal in acryogenic purification process; (6) rejection of nitrogen to increasethe composition of CO₂ in the product stream to meet pipelinerequirements (note that the nitrogen rejection and CO₂ aspects may beused together to provide improved results); and (7) catalytic combustionof hydrogen and hydrocarbons in the helium-enriched stream (with theaddition of air or oxygen) to remove impurities in the helium productstream.

Various terms have been defined above. To the extent a term used in aclaim is not defined above, it should be given the broadest definitionpersons in the pertinent art have given that term as reflected in atleast one printed publication or issued patent. Furthermore, allpatents, test procedures, and other documents cited in this applicationare fully incorporated by reference to the extent such disclosure is notinconsistent with this application for all jurisdictions in which suchincorporation is permitted.

Certain embodiments and features of the invention have been describedusing a set of numerical upper limits and a set of numerical lowerlimits. For the sake of brevity, only certain ranges are explicitlydisclosed herein. However, it should be appreciated that ranges from anylower limit to any upper limit are contemplated unless otherwiseindicated. Similarly, ranges from any lower limit may be combined withany other lower limit to recite a range not explicitly recited, andranges from any upper limit may be combined with any other upper limitto recite a range not explicitly recited. Further, a range includesevery point or individual value between its end points even though notexplicitly recited. Thus, every point or individual value may serve asits own lower or upper limit combined with any other point or individualvalue or any other lower or upper limit, to recite a range notexplicitly recited. All numerical values are “about” or “approximately”the indicated value, and take into account experimental error andvariations that would be expected by a person having ordinary skill inthe art.

In certain of the following claims, letters are used to identify claimedsteps (e.g., a., b., c., etc.). These letters are used to aid inreferring to the method steps and are not intended to indicate the orderin which the claimed steps are performed, unless and only to the extentthat such order is necessary for operability of the invention orspecifically recited in the claims.

While the foregoing is directed to embodiments of the invention andalternate embodiments thereof, various changes, modifications, andalterations from the invention may be contemplated by those skilled inthe art without departing from the intended spirit and scope thereof. Itis intended that the present invention only be limited by the terms ofthe appended claims.

1. A method for recovering helium from a feed stream containing helium,carbon dioxide and at least one of methane and nitrogen, the methodcomprising: introducing a separator feed stream into a separator, theseparator feed stream comprising at least a portion of the feed stream,separating the separator feed stream into a first helium-enriched streamand a first CO₂-enriched stream, and withdrawing the firsthelium-enriched stream and the first CO₂-enriched stream from theseparator; introducing a pressure swing adsorption unit feed stream intoa pressure swing adsorption unit, the pressure swing adsorption unitfeed stream comprising at least a portion of the first helium-enrichedstream, separating the pressure swing adsorption unit feed stream into ahelium-rich product stream and a helium-lean stream, and withdrawing thehelium-rich product stream and the helium-lean stream from the pressureswing adsorption unit; compressing a compressor feed stream in acompressor to form a compressor effluent stream, the compressor feedstream comprising the helium-lean stream and a helium-enriched permeatestream; introducing a first portion of the compressor effluent streaminto a membrane separation unit, separating the first portion of thecompressor effluent stream to form the helium-enriched permeate streamand a helium-depleted non-permeate stream, and withdrawing thehelium-enriched permeate stream and the helium-depleted non-permeatestream from the membrane separation unit; and introducing a secondportion of the compressor effluent stream into the separator.
 2. Themethod of claim 1 wherein the first portion of the compressor effluentstream has a molar flow rate, F₁, the second portion of the compressoreffluent stream has a molar flow rate, F₂, and wherein$0.60 \leq \frac{F_{1}}{F_{2}} \leq {0.85.}$
 3. The method of claim 1wherein the membrane separation unit comprises a separation modulewherein the separation module is a hollow fiber module or a spiral woundmodule.
 4. The method of claim 3 wherein the separation module comprisesa membrane, wherein the membrane comprises a support, wherein thesupport comprises a material selected from the group consisting ofpolysulfone, cellulose acetate, an aromatic polyimide, an aromaticpolyamide, an aromatic polycarbonate, poly(dimethyl phenylene oxide),poly(dimethyl siloxane), and carbon molecular sieve.
 5. The method ofclaim 4 wherein the separation membrane is a mixed matrix membrane. 6.The method of claim 4 wherein the separation membrane is a facilitatedtransport membrane.
 7. The method of claim 1 wherein the separator is apressure swing adsorption separator.
 8. The method of claim 1 whereinthe separator is a fractionator.
 9. The method of claim 8, wherein thefractionator is a distillation column, wherein the first helium-enrichedstream is withdrawn from an upper location of the distillation column,and the first CO₂-enriched stream is withdrawn from a lower location ofthe distillation column, the method further comprising the steps of:cooling the feed stream to form the separator feed stream; and feeding aliquid stream comprising CO₂ to an upper portion of the distillationcolumn as a CO₂ wash stream; wherein at least part of the separator feedstream is introduced into the distillation column at an locationintermediate the upper location of the distillation column and the lowerlocation of the distillation column.
 10. A system for recovering heliumfrom a feed stream containing helium, carbon dioxide and at least one ofmethane and nitrogen, the system comprising: a separator operativelydisposed to receive a separator feed stream, the separator feed streamcomprising at least a portion of the feed stream, the separatoroperatively configured to separate the separator feed stream into afirst helium-enriched stream and a first CO₂-enriched stream; a pressureswing adsorption unit operatively configured to separate a pressureswing adsorption unit feed stream into a helium-rich product stream anda helium-lean stream, the pressure swing adsorption unit feed streamcomprising at least a portion of the first helium-enriched stream; acompressor operatively disposed to receive a compressor feed streamcomprising the helium-lean stream and a helium-enriched permeate stream,the compressor operatively configured to compress the compressor feedstream to form a compressor effluent stream; and a membrane separationunit operatively disposed to receive a first portion of the compressoreffluent stream and operatively configured to separate the first portionof the compressor effluent stream into the helium-enriched permeatestream and a helium-depleted non-permeate stream; wherein the separatoris also operatively disposed to receive a second portion of thecompressor effluent stream.
 11. The system of claim 10 wherein themembrane separation unit comprises a separation membrane wherein theseparation membrane is a hollow fiber membrane or a spiral woundmembrane.
 12. The system of claim 11 wherein the separation membranecomprises a support, wherein the support comprises a material selectedfrom the group consisting of polysulfone, cellulose acetate, an aromaticpolyimide, an aromatic polyamide, an aromatic polycarbonate,poly(dimethyl phenylene oxide), poly(dimethyl siloxane), and carbon. 13.The system of claim 11 wherein the separation membrane is a mixed matrixmembrane.
 14. The system of claim 11 wherein the separation membrane isa facilitated transport membrane.
 15. The system of claim 10 wherein theseparator is a pressure swing adsorption separator.
 16. The system ofclaim 10 wherein the separator is a fractionator.
 17. The system ofclaim 16 wherein the fractionator is a distillation column, wherein thedistillation column has a first outlet operatively disposed to withdrawthe first helium-enriched stream, the first outlet located in an upperportion of the distillation column; wherein the distillation column hasa second outlet operatively disposed to withdraw the first CO₂-enrichedstream, the second outlet located in a lower portion of the distillationcolumn; wherein the distillation column has a first inlet operativelydisposed to introduce the separator feed stream, the first inlet locatedat a position intermediate the upper portion of the distillation columnand the lower portion of the distillation column; wherein thedistillation column has a second inlet operatively disposed to introducea CO₂ wash stream, the second inlet located in the upper portion of thedistillation column; the system further comprising: one or more heatexchangers operatively configured to cool the at least a portion of thefeed stream to form the separator feed stream by indirect heat transferwith a portion or all of the first helium-enriched stream and a portionor all of the first CO₂-enriched stream thereby heating the portion orall of the first helium-enriched stream and the portion or all of thefirst CO₂-enriched stream.
 18. The system of claim 10, wherein the firsthelium-enriched stream comprises one or more combustible components, thesystem further comprising a catalytic combustor operatively configuredto combust the one or more combustible components in the firsthelium-enriched stream in the presence of oxygen to at least partiallyconvert the combustible components to CO₂ and H₂O thereby forming acombustible component-depleted helium-enriched stream wherein thepressure swing adsorption unit feed stream comprises the combustiblecomponent-depleted helium-enriched stream as the at least a portion ofthe first helium-enriched stream.